A high carbon chain aldehyde oxidation reaction and separation combined system

Abstract

The application discloses a high-carbon-chain aldehyde oxidation reaction and separation combined system, which comprises a liquid-liquid mixer, a feed and product heat exchanger, a gas-liquid mixer, an oxidation reactor, an air compressor, an air purifier, an air and catalyst heat exchanger, a waste gas cooler, a waste gas separation tank, a reaction product buffer tank, a reaction product booster pump, a heavy component removal tower, a heavy component removal tower top cooler, a heavy component removal tower top reflux tank, a heavy component removal tower top reflux pump, a heavy component removal tower bottom reboiler, a heavy component removal tower bottom pump, a light component removal tower, a light component removal tower top cooler, a light component removal tower top reflux tank, a light component removal tower top reflux pump, a light component removal tower bottom reboiler, a light component removal tower bottom pump, a product cooler, a high-boiling substance cooler, a vacuum pump and a waste gas treatment facility. The application has the advantages of high reaction conversion rate, good reaction selectivity, high purity of target products, greatly improved catalyst recycling rate and reduced comprehensive operation cost.

Description

TECHNICAL FIELD

[0001] The present application relates to a high carbon chain aldehyde oxidation reaction and separation combined system, belonging to the technical field of chemical reaction system equipment. BACKGROUND

[0002] High carbon chain organic acids such as isononyl acid are widely used, which can be used as a raw material for synthetic lubricants, a pharmaceutical intermediate, a raw material for metal soap and metal processing fluid, and is also suitable for modification of alkyd resin, which can improve the yellowing resistance and impact resistance, and can also be used to produce various isononyl acid esters, which can be used in the field of cosmetics, and its metal salt can be used in different purposes such as paint drier, vinyl stabilizer, polyvinyl chloride stabilizer and preservative, tire adhesion aid, etc.

[0003] Oxidation of high carbon chain aldehyde is the main production process of acid, at present, metal salt homogeneous catalyst is mostly used in aldehyde oxidation to produce acid, which mainly functions to promote oxidation and quickly decompose peracid generated by reaction to prevent accumulation and explosion of peracid. However, metal salt can promote the formation of free radicals, accelerate chain reaction, shorten the induction period of reaction, and significantly shorten the reaction time. With the rapid development of exothermic reaction, the reaction is difficult to control, and the selectivity is reduced. At the same time, in the reaction process, iron and other metal ions will accumulate in the material in the metal reactor and pipeline through multiple material circulation, which promotes the initiation of reaction, leading to too fast reaction and rapid increase of heat release rate, and the temperature is difficult to control. The peroxide decomposition catalyst used in the prior art is a homogeneous catalyst, which has low concentration and is difficult to separate, and there is a risk of slagging, plugging and explosion in the distillation column.

[0004] In summary, in the prior art of high carbon chain aldehyde oxidation reaction for preparing corresponding carboxylic acid, a homogeneous metal salt catalyst is usually added in the oxidation reactor to accelerate the reaction and decomposition of peroxide, but with the progress of oxidation reaction, iron and other metal ions will accumulate in the system, leading to reduced selectivity of reaction, increased by-products, low conversion rate of reaction, and difficulty in separation of metal ions. At the same time, there are problems such as high boiling point of high carbon chain hydrocarbon, difficulty in separation by ordinary rectification, low purity of target product, non-recovery of catalyst, high operation cost, etc. SUMMARY

[0005] The technical problem to be solved by the present application is to provide a high carbon chain aldehyde oxidation reaction and separation combined system for the oxidation reaction of high carbon aldehyde to produce high carbon acid, which can improve the conversion rate, selectivity of oxidation reaction and purity of high carbon acid under the premise of using homogeneous metal salt catalyst, and can efficiently recover the catalyst in the reaction process, reduce the loss of metal salt catalyst, reduce the operation cost, and increase the economic benefit.

[0006] In order to solve the above technical problems, the present application realizes the following technical scheme:

[0007] A high carbon chain aldehyde oxidation reaction and separation combined system, comprising:

[0008] Liquid-liquid mixer for raw material feeding: the outlet end of the liquid-liquid mixer is communicated with the gas-liquid mixer;

[0009] Oxidation reactor for reaction: the top of the oxidation reactor is provided with a gas outlet, and one side of the upper portion is provided with a reflux port and a discharge port; the bottom of the oxidation reactor is provided with an ultra-micro bubble distributor, and the ultra-micro bubble distributor is provided with an air distributor;

[0010] Air compressor: the outlet end of the air compressor is respectively communicated with the air distributor and the gas-liquid mixer, and the outlet end of the gas-liquid mixer is communicated with the ultra-micro bubble distributor;

[0011] Waste gas separation tank: one side of the waste gas separation tank is provided with an air inlet, the top is provided with a gas outlet, and the bottom is provided with a discharge port; the gas outlet of the oxidation reactor is communicated with the air inlet of the waste gas separation tank through a waste gas cooler, the gas outlet of the waste gas separation tank is communicated with a waste gas treatment device, and the discharge port of the waste gas separation tank is communicated with the reflux port of the oxidation reactor; the waste gas is discharged into the atmosphere after being treated by the waste gas treatment device;

[0012] Reaction product buffer tank: the top of the reaction product buffer tank is provided with an inlet and a gas outlet, and the bottom is provided with a discharge port and a reaction product buffer tank dehydration hopper drain pipe; the inlet of the reaction product buffer tank is communicated with the discharge port of the oxidation reactor, and the gas outlet of the reaction product buffer tank is communicated with the waste gas treatment device;

[0013] De-heavy tower: one side of the de-heavy tower is provided with an inlet, the top is provided with a gas outlet, one side of the upper portion is provided with a reflux port, and the bottom is provided with a discharge port; the discharge port of the reaction product buffer tank is communicated with the inlet of the de-heavy tower through a reaction product booster pump, and the discharge port of the de-heavy tower is communicated with a high-boiling tube and a liquid-liquid mixer through a de-heavy tower bottom pump; the bottom of the de-heavy tower is connected to a heat source through a de-heavy tower bottom reboiler;

[0014] De-light tower: one side of the de-light tower is provided with an inlet, the top is provided with a gas outlet, one side of the upper portion is provided with a reflux port, and the bottom is provided with a discharge port; the discharge port of the de-light tower is communicated with a product outlet pipe through a de-light tower bottom pump for discharging; the bottom of the de-light tower is connected to a heat source through a de-light tower bottom reboiler;

[0015] De-heavy tower top reflux tank: the top of the de-heavy tower top reflux tank is provided with an inlet and a gas outlet, and the bottom is provided with a discharge port; the gas outlet of the de-heavy tower is communicated with the inlet of the de-heavy tower top reflux tank through a de-heavy tower top cooler, the gas outlet of the de-heavy tower top reflux tank is communicated with the waste gas treatment device through a vacuum pump, and the discharge port of the de-heavy tower top reflux tank is communicated with the reflux port of the de-heavy tower and the inlet of the de-light tower through a de-heavy tower top reflux pump;

[0016] The top reflux tank of the light removal tower is provided with a feed inlet and a gas outlet at the top, and a discharge outlet and a dehydration hopper drain pipe of the top reflux tank of the light removal tower at the bottom. The gas outlet of the light removal tower is communicated with the feed inlet of the top reflux tank of the light removal tower through a top cooler of the light removal tower. The gas outlet of the top reflux tank of the light removal tower is communicated with a waste gas treatment device through a vacuum pump. The discharge outlet of the top reflux tank of the light removal tower is communicated with the reflux port of the light removal tower, a C8 / C9 mixed pipe and a liquid-liquid mixer through a top reflux pump of the light removal tower.

[0017] Preferably, the liquid-liquid mixer is communicated with a liquid-liquid mixer inlet pipe and a catalyst supplement pipe, respectively.

[0018] Preferably, the outside of the oxidation reactor is provided with a jacket, and the inside is provided with an oxidation reactor cooling coil.

[0019] Preferably, the outlet end of the air compressor is provided with an air purifier.

[0020] Preferably, a product cooler is arranged on the product outlet pipe, and a high-boiling substance cooler is arranged on the high-boiling substance pipe.

[0021] Preferably, the connecting pipelines between the heavy removal tower bottom pump and the liquid-liquid mixer and between the air compressor and the gas-liquid mixer are heat-exchanged through an air / catalyst heat exchanger.

[0022] Preferably, the connecting pipeline between the liquid-liquid mixer and the gas-liquid mixer and the product outlet pipe are heat-exchanged through a feed / product heat exchanger.

[0023] Compared with the prior art, the application has the following beneficial effects:

[0024] The single-pass conversion rate of high-carbon-chain aldehyde is greater than or equal to 90%, the selectivity of target high-carbon acid is greater than or equal to 92%, and the purity of high-carbon acid is greater than or equal to 99%;

[0025] The reaction condition is mild, the reaction temperature is less than or equal to 85 DEG C, and the reaction pressure is less than or equal to 0.1 MPa;

[0026] The vacuum rectification mode is adopted, the boiling point of the rectification medium and the bottom temperature of the rectification tower are reduced, the rectification precision is ensured, and then the catalyst recovery rate is ensured. At the initial stage of operation, the catalyst recovery rate is greater than or equal to 95%, and the activity of the recovered catalyst is greater than or equal to 85%.

[0027] The air utilization rate is increased by 25% by adopting the super-micro bubble technology.

[0028] The VOCs content in the waste gas reaches the national standard by adopting the waste gas treatment facility through the zeolite molecular sieve rotating adsorption technology, and the concentrated VOCs adsorbed can be sent to a flare incinerator.

[0029] The reaction condition is mild, the catalyst recovery rate is high, the operation cost of the device is reduced, and the cost can be reduced by more than 15%. Attached Figure Description

[0030] Figure 1 This is a schematic diagram of the high-carbon chain aldehyde oxidation reaction and separation combination system provided by the present invention. Detailed Implementation

[0031] To make the present invention more apparent and understandable, preferred embodiments are described in detail below with reference to the accompanying drawings.

[0032] Example

[0033] like Figure 1 As shown, this invention provides a combined system for the oxidation reaction and separation of high-carbon chain aldehydes, comprising:

[0034] Liquid-liquid mixer 1 for raw material feeding: The inlet end of liquid-liquid mixer 1 is connected to liquid-liquid mixer inlet pipe 28 and catalyst replenishment pipe 44; the outlet end of liquid-liquid mixer 1 is connected to liquid-liquid mixer outlet pipe 29, and liquid-liquid mixer outlet pipe 29 is connected to feed / product heat exchanger outlet pipe 30 after passing through feed / product heat exchanger 2, and feed / product heat exchanger outlet pipe 30 is connected to the inlet end of gas-liquid mixer 3;

[0035] Oxidation reactor 4 for reaction: The top of oxidation reactor 4 is provided with an air outlet, and the upper side is provided with a reflux outlet and a discharge outlet; the bottom of oxidation reactor 4 is provided with an ultra-micro bubble distributor 32, and an air distributor 60 is provided on the ultra-micro bubble distributor 32; the outside of oxidation reactor 4 is provided with a jacket, and the inside is provided with an oxidation reactor cooling coil 71. The bottom of the jacket is provided with an oxidation reactor jacket cold source inlet pipe 72, and the top is provided with an oxidation reactor jacket cold source outlet pipe 73. The two ends of the oxidation reactor cooling coil 71 are respectively oxidation reactor coil cold source inlet pipe 75 and oxidation reactor coil cold source outlet pipe 76. The oxidation reactor coil cold source inlet pipe 75 and oxidation reactor coil cold source outlet pipe 76 are connected from the outside of oxidation reactor 4, and the oxidation reactor coil cold source inlet pipe 75 is below the oxidation reactor coil cold source outlet pipe 76.

[0036] Air compressor 5: the inlet end of air compressor 5 is communicated with the atmosphere, the outlet end is connected with air purifier 6 through air compressor outlet pipe 56, the impurities such as oil and dust in the air are removed through air purifier 6, the outlet end of air purifier 6 is connected with air / catalyst heat exchanger 7 through air purifier outlet pipe 57, the outlet end of air / catalyst heat exchanger 7 is communicated with air / catalyst heat exchanger outlet pipe 58, air / catalyst heat exchanger outlet pipe 58 is divided into two ways, one way is connected with air distributor 60 through air supplement pipe 59, the other way is connected with the inlet end of gas-liquid mixer 3 through mixer inlet pipe 61, the outlet end of gas-liquid mixer 3 is communicated with ultramicro bubble distributor 32 through gas-liquid mixer outlet pipe 31, ultramicro bubble distributor 32 is arranged in the inside of oxidation reactor 4;

[0037] Waste gas separation tank 9: one side of waste gas separation tank 9 is provided with gas inlet, the top is provided with gas outlet, the bottom is provided with discharge port, the gas outlet of oxidation reactor 4 is communicated with the gas inlet of waste gas separation tank 9 through oxidation reactor gas phase pipe 62, waste gas cooler 8 and waste gas cooler outlet pipe 63 in sequence, the gas outlet of waste gas separation tank 9 is communicated with waste gas treatment device 27 through reaction product buffer tank gas phase pipe 69 and vacuum pump outlet pipe 70 in sequence, the discharge port of waste gas separation tank 9 is communicated with the reflux port of oxidation reactor 4 through waste gas separation tank bottom liquid phase pipe 64;

[0038] Reaction product buffer tank 10: the top of reaction product buffer tank 10 is provided with feed inlet and gas outlet, the bottom is provided with discharge port and reaction product buffer tank dehydration hopper drain pipe 78, the feed inlet of reaction product buffer tank 10 is communicated with the discharge port of oxidation reactor 4 through product outlet pipe 33, the gas outlet of reaction product buffer tank 10 is communicated with vacuum pump outlet pipe 70 through reaction product buffer tank gas phase pipe 68;

[0039] The heavy-removing tower 12 is provided with a feed inlet on one side, a gas outlet at the top, a reflux inlet at the upper part, and a discharge outlet at the bottom. The discharge outlet of the reaction product buffer tank 10 is connected to the feed inlet of the heavy-removing tower 12 in sequence through a reaction product booster pump feed pipe 34, a reaction product booster pump 11, and a reaction product booster pump outlet pipe 35. The discharge outlet of the heavy-removing tower 12 is connected to a heavy-removing tower bottom pump 17 through a heavy-removing tower bottom outlet pipe 41. The outlet end of the heavy-removing tower bottom pump 17 is connected to a heavy-removing tower bottom pump outlet pipe 42. The heavy-removing tower bottom pump outlet pipe 42 is connected to an air / catalyst heat exchanger outlet pipe 43 after passing through the air / catalyst heat exchanger 7, and then is divided into two paths. One path is connected to a high-boiling substance pipe 45, a high-boiling substance cooler 25, and a high-boiling substance cooler outlet pipe 46 in sequence. The other path is connected to the inlet end of the liquid-liquid mixer 1. The bottom of the heavy-removing tower 12 is connected to the heavy-removing tower bottom reboiler 16 as a heat source through a heavy-removing tower bottom reboiler oil gas inlet pipe 83 and a heavy-removing tower bottom reboiler oil gas outlet pipe 84. The heavy-removing tower bottom reboiler 16 is provided with a heavy-removing tower bottom reboiler heat source inlet pipe 79 and a heavy-removing tower bottom reboiler heat source outlet pipe 80.

[0040] The light-removing tower 18 is provided with a feed inlet on one side, a gas outlet at the top, a reflux inlet at the upper part, and a discharge outlet at the bottom. The discharge outlet of the light-removing tower 18 is connected to a light-removing tower bottom pump outlet pipe 52, a light-removing tower bottom pump 23, and a light-removing tower bottom pump outlet pipe 53 in sequence. The light-removing tower bottom pump outlet pipe 53 is connected to a feed / product heat exchanger outlet pipe 54 after passing through a feed / product heat exchanger 2, and then is connected to a product cooler 24 and a product outlet pipe 55 to send the product out. The bottom of the light-removing tower 18 is connected to a light-removing tower bottom reboiler 22 as a heat source through a light-removing tower bottom reboiler oil gas inlet pipe 85 and a light-removing tower bottom reboiler oil gas outlet pipe 86. The light-removing tower bottom reboiler 22 is provided with a light-removing tower bottom reboiler heat source inlet pipe 81 and a light-removing tower bottom reboiler heat source outlet pipe 82.

[0041] The heavy-removing tower top reflux tank 14 is provided with a feed inlet and a gas outlet at the top, and a discharge outlet at the bottom. The gas outlet of the heavy-removing tower 12 is connected to the feed inlet of the heavy-removing tower top reflux tank 14 in sequence through a heavy-removing tower top gas phase pipe 36, a heavy-removing tower top cooler 13, and a heavy-removing tower top cooler outlet pipe 37. The gas outlet of the heavy-removing tower top reflux tank 14 is connected to a vacuum pump inlet pipe 67 through a heavy-removing tower top reflux tank gas phase pipe 65. The outlet end of a vacuum pump 26 is connected to a waste gas treatment device 27 through a vacuum pump outlet pipe 70. The discharge outlet of the heavy-removing tower top reflux tank 14 is connected to a heavy-removing tower top reflux pump 15 through a heavy-removing tower top reflux tank bottom liquid phase pipe 38. The outlet end of the heavy-removing tower top reflux pump 15 is connected to a heavy-removing tower reflux pipe 39 and a light-removing tower feed pipe 40, which are connected to the reflux inlet of the heavy-removing tower 12 and the feed inlet of the light-removing tower 18, respectively.

[0042] The top of the light-removing column top reflux tank 20 is provided with a feed inlet and a gas outlet, and the bottom is provided with a discharge outlet and a light-removing column top reflux tank dewatering hopper drain pipe 74; the gas outlet of the light-removing column 18 is sequentially communicated with the light-removing column top gas pipe 47, the light-removing column top cooler 19, the light-removing column top cooler cooling pipe 48 and the feed inlet of the light-removing column top reflux tank 20; the gas outlet of the light-removing column top reflux tank 20 is sequentially communicated with the light-removing column top reflux tank gas phase pipe 66, the vacuum pump inlet pipe 67 and the inlet end of the vacuum pump 26; the discharge outlet of the light-removing column top reflux tank 20 is communicated with the light-removing column top reflux pump 21 through the light-removing column top reflux tank bottom liquid phase pipe 49; the outlet end of the light-removing column top reflux pump 21 is divided into three paths, one path is communicated with the light-removing column 18 through the light-removing column reflux pipe 50, another path is communicated with the C8 / C9 mixed pipe 51, and the third path is communicated with the inlet end of the liquid-liquid mixer 1 through the C8 / C9 return pipe.

[0043] The reaction conversion rate is high, the reaction selectivity is good, the purity of the target product is high, the catalyst recovery rate is improved, and the operation cost is reduced.

[0044] The present application adopts a bubble reactor, a mixture of high-carbon aldehyde and air enters the bottom of the reactor, and the air and high-carbon aldehyde are fully combined into micro-nano bubbles with a diameter of 10 microns to hundreds of nanometers in the reactor through an ultra-micro bubble distributor, effectively increasing the reaction area between the two, increasing the utilization rate of air by 25%, reducing the need to increase the existing system load and the risk of explosion when using pure oxygen as an oxidizing agent, and ensuring the residence time requirement due to the increase of the contact area of the reaction materials, thereby improving the single-pass conversion rate of the reaction to more than 90% under the action of the catalyst, and increasing the reaction selectivity to 92%, and the equipment volume is not significantly increased; since the oxidation reaction is an exothermic reaction, the lower the temperature, the more conducive to the reaction, the cooling coil is arranged in the reactor and the cooling jacket with a flow channel is arranged on the shell, and the reaction temperature is controlled below 85 DEG C, which more completely removes the heat generated during the reaction, and ensures the smooth completion of the oxidation reaction.

[0045] Generally, due to the high boiling point of high-carbon hydrocarbons, when high-carbon hydrocarbons and catalysts are separated by distillation, the temperature at the bottom of the distillation column is too high, the heat source temperature is higher, and an appropriate heat source needs to be additionally arranged, resulting in an increase in operation and investment; after adopting the method of vacuum distillation, the whole distillation column pressure distribution is reduced through vacuum in the vacuum light-removing distillation column, and the boiling point of high-carbon hydrocarbons is reduced accordingly, and the bottom temperature is also reduced, so that the more common steam heat source in the refinery can be used, effectively improving the service life of the catalyst, reducing daily consumption, and maximizing investment and operating costs; the vacuum light-removing distillation column effectively reduces the boiling point of the medium by using vacuum, realizes efficient separation of high-carbon aldehyde and high-carbon acid, and makes the purity of the product high-carbon acid ≥99%.

[0046] In order to reduce the increase of investment and operation cost caused by pure oxygen, and overall consider the system safety, the air in the place is taken, an air purifier is arranged at the outlet of the compressor, the dust particles in the air are reduced to below 1 mu, the oil in the air is reduced to below 1 ppmw, and the micro-nano generator for generating ultra-micro bubbles is combined, so that the utilization rate of the air is more effectively improved;

[0047] Since the oxygen in the air is used to oxidize the high-carbon aldehyde, a large amount of inert waste gas (CO2, N2, etc.) is generated, and there are volatile organic compound (VOCs) gases in the waste gas, so the VOCs gases must be treated to meet the emission standard and be discharged into the atmosphere. The non-condensable waste gas is collected by a vacuum pump and sent to a waste gas treatment facility after being collected. The waste gas treatment facility adopts a zeolite molecular sieve runner technology, the zeolite molecular sieve runner is divided into three functional areas of adsorption area, desorption area and cooling area, each area is separated by heat-resistant and solvent-resistant sealing materials, and the zeolite molecular sieve runner continuously operates in each functional area. Its working principle is that when the waste gas is sent to the adsorption area of the zeolite molecular sieve runner by the adsorption fan through the pre-filter, the zeolite runner removes the VOCs in the organic waste gas by adsorption of the zeolite molecular sieve in the adsorption area, and the purified VOCs are discharged from the chimney through the zeolite molecular sieve runner. The VOCs adsorbed in the molecular sieve runner reach the desorption area during the rotation of the runner, and are desorbed and concentrated under certain temperature conditions by small-amount hot air treatment, and the concentration multiple is generally 5-40 times. The low-concentration and large-flow organic waste gas is concentrated into high-concentration and small-flow concentrated gas, and enters the flare system. The continuous circulation work makes the VOCs content in the exhaust gas meet the national standard;

[0048] The oxidation reaction adopts a homogeneous metal salt catalyst, and for a long time, the catalyst is directly discharged without recycling, which increases the operation cost. The catalyst is separated from the product by pressure rectification in the application, the recycling rate of the catalyst is improved, a catalyst recycling and supplementing system is arranged, the use concentration of the catalyst is maximally ensured, the catalyst recovery rate is greater than or equal to 95% at the initial stage of starting, and the activity of the recovered catalyst is greater than or equal to 85%. Meanwhile, in order to effectively reduce the generation of metal ions such as iron in the reaction process, cause the blockage of pipelines and equipment, and reduce the conversion rate and selectivity of the reaction, the equipment and pipelines in the reaction part are made of stainless steel, so that the damage of the metal ions generated by oxidation to the system is reduced. Although the improvement of the equipment and pipeline materials has a certain influence on the investment, the overall operation cost of the system is still reduced by 5%-15% in the application.

Claims

1. A high carbon chain aldehyde oxidation reaction and separation combined system, characterized in that, The utility model relates to a kind of production of high-boiling point product and light component from waste gas, comprising: Liquid-liquid mixer (1) for raw material feeding, the outlet end of liquid-liquid mixer (1) is communicated with gas-liquid mixer (3); Oxidation reactor (4) for reaction: the top of oxidation reactor (4) is equipped with gas outlet, and one side of upper portion is equipped with reflux port and discharge port;The bottom in oxidation reactor (4) is equipped with ultra-micro bubble distributor (32), and air distributor (60) is equipped on ultra-micro bubble distributor (32); Air compressor (5): the outlet end of air compressor (5) is respectively communicated with air distributor (60), gas-liquid mixer (3), and the outlet end of gas-liquid mixer (3) is communicated with ultra-micro bubble distributor (32); Waste gas separation tank (9): one side of waste gas separation tank (9) is equipped with air inlet, and the top is equipped with gas outlet, and the bottom is equipped with discharge port, and the gas outlet of oxidation reactor (4) is communicated with the air inlet of waste gas separation tank (9) through waste gas cooler (8), and the gas outlet of waste gas separation tank (9) is communicated with waste gas treatment device (27), and the discharge port of waste gas separation tank (9) is communicated with the reflux port of oxidation reactor (4); Reaction product buffer tank (10): the top of reaction product buffer tank (10) is equipped with feed inlet and gas outlet, and the bottom is equipped with discharge port and reaction product buffer tank dehydration hopper drain pipe (78), and the feed inlet of reaction product buffer tank (10) is communicated with the discharge port of oxidation reactor (4), and the gas outlet of reaction product buffer tank (10) is communicated with waste gas treatment device (27); Deheavy tower (12): one side of deheavy tower (12) is equipped with feed inlet, and the top is equipped with gas outlet, and one side of upper portion is equipped with reflux port, and the bottom is equipped with discharge port, and the discharge port of reaction product buffer tank (10) is communicated with the feed inlet of deheavy tower (12) through reaction product booster pump (11), and the discharge port of deheavy tower (12) is respectively communicated with high-boiling point pipe (45) and liquid-liquid mixer (1) through deheavy tower bottom pump (17);The bottom of deheavy tower (12) is connected heat source through deheavy tower bottom reboiler (16); De-light tower (18): one side of de-light tower (18) is equipped with feed inlet, and the top is equipped with gas outlet, and one side of upper portion is equipped with reflux port, and the bottom is equipped with discharge port, and the discharge port of de-light tower (18) is communicated with product outlet pipe (55) through de-light tower bottom pump (23) and is discharged;The bottom of de-light tower (18) is connected heat source through de-light tower bottom reboiler (22); Deheavy tower top reflux tank (14): the top of deheavy tower top reflux tank (14) is equipped with feed inlet and gas outlet, and the bottom is equipped with discharge port, and the gas outlet of deheavy tower (12) is communicated with the feed inlet of deheavy tower top reflux tank (14) through deheavy tower top cooler (13), and the gas outlet of deheavy tower top reflux tank (14) is communicated with waste gas treatment device (27) through vacuum pump (26), and the discharge port of deheavy tower top reflux tank (14) is respectively communicated with the reflux port of deheavy tower (12) and the feed inlet of de-light tower (18) through deheavy tower top reflux pump (15); The light removal tower top reflux tank (20) is provided with a feed inlet and a gas outlet at the top and a discharge outlet and a dehydration hopper drain pipe (74) at the bottom. The gas outlet of the light removal tower (18) is communicated with the feed inlet of the light removal tower top reflux tank (20) through a light removal tower top cooler (19). The gas outlet of the light removal tower top reflux tank (20) is communicated with a waste gas treatment device (27) through a vacuum pump (26). The discharge outlet of the light removal tower top reflux tank (20) is communicated with the reflux port of the light removal tower (18), a C8 / C9 mixed pipe (51) and a liquid-liquid mixer (1) through a light removal tower top reflux pump (21).

2. The high carbon chain aldehyde oxidation reaction and separation combined system of claim 1, wherein, The liquid-liquid mixer (1) is communicated with a liquid-liquid mixer inlet pipe (28) and a catalyst supplement pipe (44).

3. The high carbon chain aldehyde oxidation reaction and separation combined system of claim 1, wherein, The oxidation reactor (4) is provided with a jacket on the outside and an oxidation reactor cooling coil (71) in the inside.

4. The high carbon chain aldehyde oxidation reaction and separation combined system of claim 1, wherein, The outlet end of the air compressor (5) is provided with an air purifier (6).

5. The high carbon chain aldehyde oxidation reaction and separation combined system of claim 1, wherein, A product cooler (24) is arranged on the product outlet pipe (55), and a high-boiling substance cooler (25) is arranged on the high-boiling substance pipe (45).

6. The high carbon chain aldehyde oxidation reaction and separation combined system of claim 1, wherein, The connecting pipelines between the light removal tower bottom pump (17) and the liquid-liquid mixer (1) and between the air compressor (5) and the gas-liquid mixer (3) are heat-exchanged through an air / catalyst heat exchanger (7).

7. The high carbon chain aldehyde oxidation reaction and separation combined system of claim 1, wherein, The connecting pipelines between the liquid-liquid mixer (1) and the gas-liquid mixer (3) and the product outlet pipe (55) are heat-exchanged through a feed / product heat exchanger (2).

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