A separation device and separation method for carbonyl synthesis of butyraldehyde

Abstract

This invention discloses a separation device and method for the carbonyl synthesis of butyraldehyde. Compared with the prior art which only involves two separations, this invention sets up a stripping tower for primary screening, a flash evaporator for secondary screening, and a stabilizing tower for tertiary screening, making the separation more rational and resulting in higher purity of the butyraldehyde solution. During the flash evaporator secondary screening, the primary screening mixture enters the flash evaporator tangentially to complete the first separation, then passes through two plate filter discs to complete the second separation. The rising mixed gas contacts the conical filter disc to achieve the third separation, and the rising mixed gas passes through the sprayed secondary screening mixture to achieve the fourth separation. Finally, the catalyst is thoroughly screened out through four separations. Compared with the high-precision filters used in the prior art, this invention improves the filtration effect by setting up multiple separations, replacing the evaporator trap, eliminating the need for high-precision components, and reducing costs, making it easier to promote and use.

Description

Technical Field

[0001] The invention relates to the technical field of butyraldehyde separation, and in particular to a separation device and a separation method for carbonyl synthesis of butyraldehyde. Background Art

[0002] The carbonyl synthesis method is one of the commonly used methods for synthesizing butyraldehyde, which uses olefins as raw materials and reacts with synthesis gas in the presence of a catalyst to generate an aldehyde having one more carbon atom than the original olefin. After the reaction is completed, the discharged mixed liquid contains propylene, propane, catalyst and butyraldehyde. The existing separation method is to first heat the mixed liquid and then send it to a high-pressure evaporation trap for primary separation. Most of the propylene and propane are vaporized and discharged, while the remaining mixed liquid is mainly composed of catalyst and butyraldehyde. After being discharged from the bottom of the high-pressure evaporation trap, it is heated again and sent to a low-pressure evaporation trap. Butyraldehyde is vaporized and discharged, and the remaining liquid catalyst is discharged and reused. After butyraldehyde is vaporized, it still contains a small amount of propylene and propane. Therefore, the gaseous butyraldehyde will be passed into a condenser, and propylene and propane will still remain in the gaseous state and be discharged, while the gaseous butyraldehyde will be liquefied and then flow into a propylene absorption tower for treatment to complete the separation of butyraldehyde.

[0003] However, high-precision filters are required in high-pressure evaporation collectors and low-pressure evaporation collectors to prevent fine droplets from being entrained by steam and escaping during the evaporation process. Therefore, the existing separation devices have high precision requirements and high equipment costs, which is not conducive to promotion and use. Summary of the invention

[0004] In view of the above-mentioned defects or deficiencies in the prior art, it is desirable to provide a separation device and a separation method for carbonyl synthesis of butyraldehyde.

[0005] In a first aspect, the present invention provides a separation device for carbonyl synthesis of butyraldehyde, comprising:

[0006] A stripping tower, wherein the top is provided with a first liquid inlet connected to the outlet of the butyraldehyde reactor, the bottom is provided with a first gas inlet for introducing synthesis gas, and the bottom end of the stripping tower is provided with a first liquid outlet;

[0007] A flash evaporator, wherein a tangential liquid inlet pipe connected to the first liquid outlet is provided on one side of the bottom, and a second gas outlet is provided on the top. A plurality of plate filter discs are provided in the middle of the flash evaporator, and a conical filter disc is provided on the top. An annular tube is provided around the edge of the top surface of the conical filter disc, and a plurality of nozzles are evenly provided on the annular tube away from the inner wall of the flash evaporator. A busbar is provided at the position of each nozzle on the top conical surface of the conical filter disc corresponding to the position of each nozzle, and the direction of water flow sprayed by each nozzle is parallel to the extension direction of the busbar. A reflux pipe connected to the annular tube is provided on the side wall of the flash evaporator;

[0008] A shell and tube condenser, wherein the top end is provided with a shell-side air inlet connected to the second air outlet, the bottom end is provided with a shell-side liquid outlet, a tee is provided below the shell-side liquid outlet, a first opening of the tee is connected to the shell-side liquid outlet, and a second opening of the tee is connected to the reflux pipe;

[0009] A stabilizing tower has a third liquid inlet at the bottom which is connected to the third opening of the three-way pipe. The stabilizing tower is used for final separation of propylene, propane, butyraldehyde and catalyst.

[0010] According to the technical solution provided in the embodiment of the present application, the stabilizing tower further includes:

[0011] A heating part is arranged at the bottom of the stabilizing tower, comprising a filler arranged inside the stabilizing tower and a jacket wrapped outside the stabilizing tower, wherein heat transfer oil flows in the jacket;

[0012] A cooling part is arranged at the top of the stabilizing tower, comprising a lower box arranged at the top of the stabilizing tower, a first gap is provided in the middle of the lower box, an upper box is arranged above the lower box, a second gap is provided between the upper box and the inner wall of the stabilizing tower, a plurality of condensing pipes are arranged between the upper box and the lower box, and the two are connected through the condensing pipes, an annular baffle is arranged at the top of the lower box around the first gap, and condensed water flows in the lower box and the upper box;

[0013] The pipe mouth portion includes a third gas outlet arranged at the top end of the stabilizing tower, a fourth liquid outlet arranged at the bottom end of the stabilizing tower, and a third liquid outlet arranged at a position of the annular baffle corresponding to the side wall of the stabilizing tower.

[0014] According to the technical solution provided in the embodiment of the present application, the liquid inlet direction of the tangential liquid inlet pipe is tangent to the arc surface of the inner wall of the flash evaporator.

[0015] According to the technical solution provided in the embodiment of the present application, a heater is further provided between the first liquid outlet and the tangential liquid inlet pipe, the heater inlet is connected to the first liquid outlet, and the heater outlet is connected to the tangential liquid inlet pipe.

[0016] According to the technical solution provided in the embodiment of the present application, a first gas outlet is provided at the top of the stripping tower, and a shell-side gas outlet is provided at the top of the shell and tube condenser. Both the first gas outlet and the shell-side gas outlet are connected to the interior of the butyraldehyde reactor.

[0017] According to the technical solution provided in the embodiment of the present application, a liquid return port is provided on one side of the bottom of the flash evaporator, and the liquid return port is connected to the fourth liquid outlet. A second liquid outlet is provided at the bottom end of the flash evaporator, and the second liquid outlet is connected to the inside of the butyraldehyde reactor.

[0018] According to the technical solution provided in the embodiment of the present application, a pressure pump is provided between the second liquid outlet and the butyraldehyde reactor, the pressure pump inlet is connected to the second liquid outlet, the pressure pump outlet is connected to the interior of the butyraldehyde reactor, a compressor is provided between the shell side air outlet and the butyraldehyde reactor, the compressor inlet is connected to the shell side air outlet, and the compressor outlet is connected to the interior of the butyraldehyde reactor.

[0019] In a second aspect, the present invention also provides a method for separating carbonyl-synthesized butyraldehyde, which specifically comprises the following steps:

[0020] S1. Preliminary screening, the mixed liquid is fed to the top of the stripping tower, the synthesis gas is fed to the bottom of the stripping tower, and the preliminarily screened mixed liquid and the first mixed gas are obtained;

[0021] S2. Heating: heating the pre-screened mixed solution to 140°C;

[0022] S3. Second sieve, the primary sieve mixed liquid is sent to the flash evaporator, and the first batch of catalyst solution and the second mixed gas are obtained after separation;

[0023] S4. Condensation, the second mixed gas is sent to the shell side of the shell and tube condenser, the condensate temperature is 30 ° C, and the third mixed gas and the second sieve mixed liquid are obtained after condensation;

[0024] S5. The third screen, the second screen mixed liquid is sent to the stabilization tower, and after distillation, a butyraldehyde solution, a second batch of catalyst solution and a third mixed gas are obtained.

[0025] According to the technical solution provided in the embodiment of the present application, the first mixed gas consists of propylene, propane and synthesis gas, the second mixed gas consists of propylene, propane and butyraldehyde, and the third mixed gas consists of propylene and propane.

[0026] According to the technical solution provided in the embodiment of the present application, the mixed liquid, the primary screening mixed liquid and the secondary screening mixed liquid are all composed of propylene, propane, a catalyst and butyraldehyde.

[0027] Compared with the prior art, the beneficial effects of the present invention are:

[0028] 1. Compared with the prior art which only separates twice, the present invention is provided with a stripping tower primary screen, a flash evaporator secondary screen and a stabilizing tower tertiary screen. Most of the propylene and propane are discharged through the primary screen, most of the catalyst solution is discharged through the secondary screen, and finally purified through the stabilizing tower, so that the separation is more reasonable and the purity of the butyraldehyde solution is higher;

[0029] 2. When the flash evaporator is screened twice, the pre-screened mixed liquid enters the flash evaporator along the tangential direction to form flash centrifugal separation, converting propylene, propane and butyraldehyde into gaseous state, and the liquid catalyst falls into the bottom of the flash evaporator to complete the first catalyst separation, and then passes through two plate filter discs to preliminarily intercept the catalyst solution to complete the second catalyst separation. The second screened mixed liquid is sprayed on the surface of the conical filter disc, which first reduces the temperature of the conical filter disc. Due to the difference in dew points of the components in the rising mixed gas, when the gaseous catalyst contacts the conical filter disc and flows upward along the pores, it will precipitate from the mixed gas to form a liquid state and flow into the bottom of the flash evaporator to achieve the third catalyst separation. The rising mixed gas will pass through the sprayed second screened mixed liquid, and the sprayed second screened mixed liquid will cool the rising mixed gas again to achieve the fourth catalyst separation. Finally, the catalyst is fully screened out through four separations. Compared with the high-precision filter used in the prior art, the present invention improves the filtering effect by setting multiple separations, replaces the evaporation trap, does not require high-precision components, and has lower costs and is more convenient for popularization and use;

[0030] 3. After the initial screening, most of the propylene and propane are screened out, and the first mixed gas is composed of synthesis gas, propylene and propane, without catalyst and butyraldehyde solution. Therefore, the first mixed gas can be recycled into the butyraldehyde reactor for reuse, reducing the exhaust gas and reducing the raw material consumption;

[0031] 4. The second-screen mixed liquid sprayed on the surface of the conical filter disc is condensed by a shell and tube condenser. It has a lower temperature and also contains a small amount of catalyst solution. The second-screen mixed liquid returns to the flash evaporator, which not only achieves a cooling effect but also achieves the purpose of separating the catalyst again.

[0032] It should be understood that the contents described in the summary of the invention are not intended to limit the key or important features of the embodiments of the present invention, nor are they intended to limit the scope of the present invention. Other features of the present invention will become easily understood through the following description. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] Other features, objects and advantages of the present invention will become more apparent from the detailed description of non-limiting embodiments made with reference to the following drawings:

[0034] Figure 1 A schematic structural diagram of a separation device for carbonyl synthesis of butyraldehyde provided in an embodiment of the present application.

[0035] Figure 2 A schematic diagram of the structure of a conical filter disc in a separation device for carbonyl synthesis of butyraldehyde provided in an embodiment of the present application.

[0036] Figure 3 A schematic diagram of the structure of a reflux pipe in a separation device for carbonyl synthesis of butyraldehyde provided in an embodiment of the present application.

[0037] Figure 4 A schematic diagram of the structure of a stabilization tower in a separation device for carbonyl synthesis of butyraldehyde provided in an embodiment of the present application.

[0038] Figure 5 A flow chart of the steps of a method for separating butyraldehyde from carbonyl synthesis provided in an embodiment of the present application.

[0039] Numbers in the figure:

[0040] 1. Stripping tower; 11. First liquid inlet; 12. First gas inlet; 13. First gas outlet; 14. First liquid outlet;

[0041] 2. Heater;

[0042] 3. Flash evaporator; 31. Tangential liquid inlet pipe; 32. Second gas outlet; 33. Second liquid outlet; 34. Liquid return port; 35. Reflux pipe; 36. Plate filter disc; 37. Conical filter disc; 38. Fine pores; 39. Annular pipe; 310. Nozzle;

[0043] 4. Shell and tube condenser; 41. Shell side air inlet; 42. Shell side air outlet; 43. Shell side liquid outlet; 45. Tee pipe;

[0044] 5. Stabilizing tower; 51. Third liquid inlet; 52. Third liquid outlet; 53. Third gas outlet; 54. Fourth liquid outlet; 55. Filler; 56. Jacket; 57. Lower box; 58. Condenser; 59. Upper box; 510. Annular baffle; 511. First gap; 512. Second gap;

[0045] 61. Compressor; 62. Booster pump; 7. Synthesis gas; 8. Butyraldehyde reactor; 9. Combustion pipeline network; 10. Butyraldehyde solution. DETAILED DESCRIPTION

[0046] The present invention will be further described in detail below in conjunction with the accompanying drawings and embodiments. It is to be understood that the specific embodiments described herein are only used to explain the relevant invention, rather than to limit the invention. It should also be noted that, for ease of description, only the parts related to the invention are shown in the accompanying drawings.

[0047] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other. The present invention will be described in detail below with reference to the accompanying drawings and in combination with the embodiments. Example 1

[0048] Please refer to Figure 1~Figure 4 , an embodiment of the present invention provides a separation device for carbonyl synthesis of butyraldehyde, comprising:

[0049] The stripping tower 1 has a first liquid inlet 11 at the top connected to the outlet of the butyraldehyde reactor 8, a first gas inlet 12 at the bottom for introducing the synthesis gas 7, and a first liquid outlet 14 at the bottom of the stripping tower 1; Figure 1 As shown, the butyraldehyde reactor 8 discharges a mixed liquid containing propylene, propane, a catalyst and butyraldehyde. The stripping tower 1 has a plurality of baffles inside. The synthesis gas 7 flows upward along the gaps between the baffles, and the mixed liquid flows downward along the gaps between the baffles. The synthesis gas 7 cools the mixed liquid. The boiling points of propylene and propane in the mixed liquid are relatively low. Once cooled, most of the propylene and propane will be converted from liquid to gas. As the synthesis gas 7 flows upward, a first mixed gas is formed and discharged, thereby achieving primary screening and discharging the primary screened mixed liquid.

[0050] The flash evaporator 3 has a tangential liquid inlet pipe 31 connected to the first liquid outlet 14 at one side of the bottom, a second gas outlet 32 ​​at the top, a plurality of plate filter discs 36 at the middle of the flash evaporator 3, a conical filter disc 37 at the top, an annular tube 39 around the edge of the top surface of the conical filter disc 37, a plurality of nozzles 310 are evenly arranged on the side of the annular tube 39 away from the inner wall of the flash evaporator 3, a busbar is provided at the top conical surface of the conical filter disc 37 corresponding to the positions of the nozzles 310, the water flow direction of each nozzle 310 is parallel to the extension direction of the busbar, and a reflux pipe 35 connected to the annular tube 39 is provided on the side wall of the flash evaporator 3; Figure 1 and Figure 2 As shown, the primary screened mixed liquid entering the flash evaporator 3 contains butyraldehyde and catalyst. Since the catalyst has a high boiling point, most of the butyraldehyde will evaporate into gas after entering the flash tank and be discharged upward, while the catalyst remains in liquid form. Among them, the plate filter disc 36 will perform a separation to reduce the droplet-shaped catalyst from rising with the butyraldehyde gas flow. Secondly, the solution sprayed by the nozzle 310 can reduce the temperature of the conical filter disc 37. Due to the difference in dew points of the components in the rising mixed gas, when the gaseous catalyst contacts the conical filter disc 37 and flows upward along the pores 38, it will precipitate from the mixed gas to form a liquid and flow into the bottom of the flash evaporator 3 to achieve a separation. The rising mixed gas will pass through the sprayed second screened mixed liquid, and the sprayed second screened mixed liquid will cool the rising mixed gas again, achieving another separation and retaining most of the catalyst inside the flash evaporator 3.

[0051] The shell and tube condenser 4 has a shell-side air inlet 41 connected to the second air outlet 32 ​​at the top, a shell-side liquid outlet 43 at the bottom, a tee pipe 45 is provided below the shell-side liquid outlet 43, a first opening of the tee pipe 45 is connected to the shell-side liquid outlet 43, and a second opening of the tee pipe 45 is connected to the reflux pipe 35; Figure 1As shown, the second mixed gas after flash evaporation is condensed and liquefied to form a two-sieve mixed liquid. Due to the low boiling point and difficult condensation characteristics of propylene and propane, the two-sieve mixed liquid contains residual trace propylene, propane and catalyst, mainly butyraldehyde, and the reflux pipe 35 is connected to the shell side liquid outlet 43 through the three-way pipe 45. The low-temperature two-sieve mixed liquid after condensation can be used as the spray liquid in the flash evaporator 3, which not only has a cooling effect, but also does not introduce other interference factors. In addition, this part of the two-sieve mixed liquid is refluxed into the flash evaporator 3, and is further separated to remove the catalyst in this part of the two-sieve mixed liquid.

[0052] The stabilizing tower 5 has a third liquid inlet 51 at the bottom thereof connected to the third opening of the tee pipe 45. The stabilizing tower 5 is used for final separation of propylene, propane, butyraldehyde and catalyst; Figure 1 and Figure 4 As shown, the purpose of distillation is achieved, and the remaining trace amounts of propylene, propane and catalyst are discharged to obtain a relatively pure butyraldehyde solution 10.

[0053] In some embodiments, the stabilization tower 5 further comprises:

[0054] The heating part is arranged at the bottom of the stabilizing tower 5, and includes a filler 55 arranged inside the stabilizing tower 5, and a jacket 56 wrapped outside the stabilizing tower 5, and heat transfer oil flows in the jacket 56;

[0055] The cooling part is arranged at the top of the stabilizing tower 5, and includes a lower box 57 arranged at the top of the stabilizing tower 5. The middle of the lower box 57 has a first gap 511. An upper box 59 is arranged above the lower box 57. A second gap 512 is arranged between the upper box 59 and the inner wall of the stabilizing tower 5. A plurality of condensing pipes 58 are arranged between the upper box 59 and the lower box 57, and the two are connected through the condensing pipes 58. An annular baffle 510 is arranged around the first gap 511 at the top of the lower box 57. Condensed water flows in the lower box 57 and the upper box 59.

[0056] The pipe mouth portion includes a third gas outlet 53 provided at the top of the stabilizing tower 5, a fourth liquid outlet 54 provided at the bottom of the stabilizing tower 5, and a third liquid outlet 52 provided at the side wall of the stabilizing tower 5 at a position corresponding to the annular baffle 510;

[0057] like Figure 1 and Figure 4As shown, the two-sieve mixed liquid enters the stabilization tower 5 and first flows into the filler 55. Through the heating effect of the heat transfer oil, trace amounts of propylene, propane and butyraldehyde will be vaporized, while trace amounts of catalysts are still in liquid state, thus realizing the first step of purification; thereafter, the gaseous propylene, propane and butyraldehyde will flow upward along the first gap 511, and realize heat exchange with the outer wall of the condenser 58. Propylene and propane are not easy to condense due to their low boiling points, so trace amounts of propylene and propane will continue to be discharged upward, while the gaseous butyraldehyde will be liquefied into butyraldehyde solution 10 and drip between the annular baffle 510 and the stabilization tower 5, thus realizing the second step of purification, so that the separated butyraldehyde solution 10 has a higher purity. In addition, in the second step, a small amount of propylene and propane will flow upward from the second gap 512, and then be discharged from the third air outlet 53, and sent to the combustion pipe network 9, so as to achieve the purpose of reuse.

[0058] In some embodiments, the liquid inlet direction of the tangential liquid inlet pipe 31 is tangent to the arc surface of the inner wall of the flash evaporator 3; Figure 1 and Figure 3 As shown, when the pre-screened mixed liquid enters the flash evaporator 3, it will be centrifugally flashed along the arc surface of the inner wall of the flash evaporator 3, so that the propylene, propane and butyraldehyde in the pre-screened mixed liquid are easily vaporized and precipitated, and the catalyst will flow into the bottom of the flash evaporator 3.

[0059] In some embodiments, a heater 2 is further provided between the first liquid outlet 14 and the tangential liquid inlet pipe 31, the inlet of the heater 2 is connected to the first liquid outlet 14, and the outlet of the heater 2 is connected to the tangential liquid inlet pipe 31; Figure 1 As shown, the temperature of the pre-screened mixed liquid is increased so that propylene, propane and butyraldehyde are more easily vaporized after the pre-screened mixed liquid enters the flash evaporator 3, thereby avoiding the situation where the temperature is too low and the vaporization effect is poor.

[0060] In some embodiments, the top of the stripping tower 1 is provided with a first gas outlet 13, and the top of the shell and tube condenser 4 is provided with a shell-side gas outlet 42, and the first gas outlet 13 and the shell-side gas outlet 42 are both connected to the inside of the butyraldehyde reactor 8; Figure 1 As shown, the first mixed gas is discharged upward along the first gas outlet 13. Since the first mixed gas contains a large amount of propylene, propane and synthesis gas 7, these gases are all raw materials for the butyraldehyde reactor 8, and therefore can be returned to the butyraldehyde reactor 8 as raw material recycling, thereby improving the purpose of energy conservation and emission reduction. Similarly, the gas discharged from the shell side gas outlet 42 is mainly propylene and propane, which can also be recycled as raw materials.

[0061] In some embodiments, a liquid return port 34 is provided on one side of the bottom of the flash evaporator 3, and the liquid return port 34 is connected to the fourth liquid outlet 54. A second liquid outlet 33 is provided at the bottom of the flash evaporator 3, and the second liquid outlet 33 is connected to the inside of the butyraldehyde reactor 8; Figure 1As shown, the first batch of catalyst is separated from the flash evaporator 3, and the second batch of catalyst is discharged from the fourth liquid outlet 54 at the bottom of the stabilization tower 5. After merging into the bottom of the flash evaporator 3, the two batches of catalyst will be discharged from the second liquid outlet 33. Since the catalyst will not increase or decrease during the reaction process, it can be returned to the butyraldehyde reactor 8 for recycling.

[0062] In some embodiments, a pressure pump 62 is provided between the second liquid outlet 33 and the butyraldehyde reactor 8, the inlet of the pressure pump 62 is connected to the second liquid outlet 33, the outlet of the pressure pump 62 is connected to the inside of the butyraldehyde reactor 8, a compressor 61 is provided between the shell side gas outlet 42 and the butyraldehyde reactor 8, the inlet of the compressor 61 is connected to the shell side gas outlet 42, and the outlet of the compressor 61 is connected to the inside of the butyraldehyde reactor 8; Figure 1 As shown, in order to facilitate the input of two batches of catalysts into the butyraldehyde reactor 8, a pressure pump 62 is used to realize the driving function. Similarly, a compressor 61 is used to drive the gas to flow back to the butyraldehyde reactor 8 to avoid excessive pressure inside the butyraldehyde reactor 8 and the situation where the recovered raw materials are difficult to reflux; in addition, the driving force is provided by the synthesis gas 7 in the stripping tower 1, and there is no need to add additional driving equipment.

[0063] In some embodiments, the butyraldehyde reactor 8 can be configured as two reactors connected in series to make the reaction more complete. Furthermore, the refluxed gas and liquid are both connected to the first butyraldehyde reactor 8 , and the liquid inlet of the stripping tower 1 is connected to the liquid outlet of the second butyraldehyde reactor 8 .

[0064] In some embodiments, Figure 1 As shown, the shell and tube condenser 4 also includes a water inlet on the right and a water outlet on the left, which are used to connect to the circulating water supply pipe and the circulating water recovery pipe in the factory. Figure 4 As shown, a water inlet pipe is provided at the bottom of the lower box body 57, and a recovery pipe is provided at the top of the upper box body 59, which are respectively connected to the circulating water supply pipe and the circulating water recovery pipe in the factory to achieve the purpose of cooling water supply. Example 2

[0065] like Figure 1-Figure 5 As shown, based on a separation device for carbonyl synthesis butyraldehyde provided in Example 1, the present invention also provides a separation method for carbonyl synthesis butyraldehyde, which specifically comprises the following steps:

[0066] S1. Preliminary screening, the mixed liquid is fed to the top of the stripping tower 1, the synthesis gas is fed to the bottom of the stripping tower 1, and the preliminarily screened mixed liquid and the first mixed gas are obtained; the first mixed gas is composed of propylene, propane and synthesis gas 7, which is discharged from the top and then sent back to the butyraldehyde reactor 8 for recycling;

[0067] S2. Heating the pre-screened mixed solution to 140°C; increasing the temperature makes it easier for butyraldehyde to vaporize during subsequent flash evaporation;

[0068] S3. Second sieve, the primary sieved mixed liquid is sent to the flash evaporator 3, and the first batch of catalyst solution and the second mixed gas are obtained after separation; wherein, the pressure inside the flash evaporator 3 is about 0.3MPa, under this pressure condition, a large amount of butyraldehyde will flash out, the first batch of catalyst will be discharged from the bottom of the flash evaporator 3, and sent back to the butyraldehyde reactor 8 for recycling, and the second mixed gas is composed of propylene, propane, butyraldehyde and catalyst, wherein propylene, propane and catalyst only account for a small proportion, and butyraldehyde is the main component;

[0069] S4. Condensation, the second mixed gas is sent to the shell side of the shell and tube condenser 4, the condensed water temperature is 30°C, and after condensation, a third mixed gas and a second sieve mixed liquid are obtained; that is, butyraldehyde and trace catalysts are condensed into liquid, so the third mixed gas is mainly composed of propylene and propane, which is discharged from the shell side gas outlet 42 and sent back to the butyraldehyde reactor 8 for recycling, wherein the condensed water temperature supplied to the tube side of the shell and tube condenser 4 is about 30°C, which can cool the second mixed gas to about 40°C, at which time only propane and propylene will not be liquefied, thereby achieving the purpose of liquefying butyraldehyde and the catalyst;

[0070] S5. Three sieves, the two sieve mixed liquid is sent to the stabilization tower 5, and after distillation, a butyraldehyde solution, a second batch of catalyst solution and a third mixed gas are obtained; the second batch of catalyst solution can be refluxed to the bottom of the flash evaporator 3 and discharged together with the first batch of catalyst solution, while the third mixed gas is composed of trace amounts of propylene and propane, which is not convenient to be sent back to the butyraldehyde reactor 8, so it is directly sent to the combustion network 9 for combustion to avoid direct discharge and cause air pollution.

[0071] In some embodiments, the mixed liquor, the primary screened mixed liquor and the secondary screened mixed liquor are all composed of propylene, propane, a catalyst and butyraldehyde; the proportion of propylene, propane and the catalyst in the mixed liquor is relatively large, and compared with the mixed liquor, the proportion of propylene and propane in the primary screened mixed liquor is greatly reduced, and compared with the primary screened mixed liquor and the mixed liquor, the proportion of the catalyst in the secondary screened mixed liquor is greatly reduced.

[0072] In the description of this specification, the terms "connection", "installation", "fixation" and the like should be understood in a broad sense. For example, "connection" can be a fixed connection, a detachable connection, or an integral connection; it can be a direct connection or an indirect connection through an intermediate medium. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0073] In the description of this specification, the description of the terms "one embodiment", "some embodiments", etc. means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. In this specification, the schematic representation of the above terms does not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner.

[0074] The above are only preferred embodiments of the present application and are not intended to limit the present application. For those skilled in the art, the present application may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. A separation device for carbonyl synthesis of butyraldehyde, arranged on one side of a butyraldehyde reactor (8), characterized in that: include: A stripping tower (1) having a first liquid inlet (11) at the top thereof connected to the outlet of the butyraldehyde reaction kettle (8), a first gas inlet (12) at the bottom thereof for introducing synthesis gas (7), and a first liquid outlet (14) at the bottom end of the stripping tower (1); A flash evaporator (3), wherein a tangential liquid inlet pipe (31) connected to the first liquid outlet (14) is provided on one side of the bottom, and a second gas outlet (32) is provided on the top. A plurality of plate filter discs (36) are provided in the middle of the flash evaporator (3), and a conical filter disc (37) is provided on the top. An annular tube (39) is provided around the edge of the top surface of the conical filter disc (37). A plurality of nozzles (310) are evenly provided on the side of the annular tube (39) away from the inner wall of the flash evaporator (3). A busbar is provided at the top conical surface of the conical filter disc (37) corresponding to the positions of the nozzles (310). The direction of the water flow sprayed by each nozzle (310) is parallel to the extension direction of the busbar. A reflux pipe (35) connected to the annular tube (39) is provided on the side wall of the flash evaporator (3); A shell and tube condenser (4), wherein a shell-side air inlet (41) communicating with the second air outlet (32) is provided at the top end, a shell-side liquid outlet (43) is provided at the bottom end, a three-way pipe (45) is provided below the shell-side liquid outlet (43), a first opening of the three-way pipe (45) is communicated with the shell-side liquid outlet (43), and a second opening of the three-way pipe (45) is communicated with the reflux pipe (35); A stabilization tower (5) having a third liquid inlet (51) at its bottom which is connected to the third opening of the three-way pipe (45), the stabilization tower (5) being used for final stage separation of propylene, propane, butyraldehyde and catalyst; The stabilization tower (5) further comprises: A heating part is arranged at the bottom of the stabilization tower (5), comprising a filler (55) arranged inside the stabilization tower (5), and a jacket (56) wrapped around the outside of the stabilization tower (5), wherein heat transfer oil flows in the jacket (56); A cooling unit is arranged at the top of the stabilizing tower (5), comprising a lower box (57) arranged at the top of the stabilizing tower (5), a first gap (511) being provided in the middle of the lower box (57), an upper box (59) being provided above the lower box (57), a second gap (512) being provided between the upper box (59) and the inner wall of the stabilizing tower (5), a plurality of condensing pipes (58) being provided between the upper box (59) and the lower box (57), and the two are connected through the condensing pipes (58), an annular baffle (510) being provided at the top of the lower box (57) surrounding the first gap (511), and condensed water flowing in the lower box (57) and the upper box (59); The pipe mouth portion comprises a third gas outlet (53) arranged at the top end of the stabilizing tower (5), a fourth liquid outlet (54) arranged at the bottom end of the stabilizing tower (5), and a third liquid outlet (52) arranged at a position of the side wall of the stabilizing tower (5) corresponding to the annular baffle (510).

2. The separation device for carbonyl synthesis of butyraldehyde according to claim 1, characterized in that: The liquid inlet direction of the tangential liquid inlet pipe (31) is tangent to the arc surface of the inner wall of the flash evaporator (3).

3. The separation device for carbonyl synthesis of butyraldehyde according to claim 2, characterized in that: A heater (2) is further provided between the first liquid outlet (14) and the tangential liquid inlet pipe (31); an inlet of the heater (2) is communicated with the first liquid outlet (14), and an outlet of the heater (2) is communicated with the tangential liquid inlet pipe (31).

4. The separation device for carbonyl synthesis of butyraldehyde according to claim 3, characterized in that: The stripping tower (1) is provided with a first gas outlet (13) at the top, and the shell-side gas outlet (42) is provided with a shell-side gas outlet (42) at the top of the shell-and-tube condenser (4); the first gas outlet (13) and the shell-side gas outlet (42) are both connected to the interior of the butyraldehyde reaction kettle (8).

5. The separation device for carbonyl synthesis of butyraldehyde according to claim 4, characterized in that: A liquid return port (34) is provided at one side of the bottom of the flash evaporator (3), the liquid return port (34) being in communication with the fourth liquid outlet (54), and a second liquid outlet (33) is provided at the bottom end of the flash evaporator (3), the second liquid outlet (33) being in communication with the interior of the butyraldehyde reaction kettle (8).

6. The separation device for carbonyl synthesis of butyraldehyde according to claim 5, characterized in that: A pressure pump (62) is provided between the second liquid outlet (33) and the butyraldehyde reactor (8), the inlet of the pressure pump (62) is connected to the second liquid outlet (33), and the outlet of the pressure pump (62) is connected to the interior of the butyraldehyde reactor (8). A compressor (61) is provided between the shell-side gas outlet (42) and the butyraldehyde reactor (8), the inlet of the compressor (61) is connected to the shell-side gas outlet (42), and the outlet of the compressor (61) is connected to the interior of the butyraldehyde reactor (8).

7. The method for separating oxo-butyraldehyde according to the separation device of oxo-butyraldehyde according to any one of claims 1 to 6, characterized in that: The specific steps include: S1. Preliminary screening, sending the mixed liquid to the top of the stripping tower (1), sending the synthesis gas to the bottom of the stripping tower (1), obtaining a preliminarily screened mixed liquid and a first mixed gas; S2. Heating: heating the pre-screened mixed solution to 140°C; S3. Second sieve, the primary sieve mixed liquid is sent to the flash evaporator (3), and the first batch of catalyst solution and the second mixed gas are obtained after separation; S4. Condensation, the second mixed gas is sent to the shell side of the shell and tube condenser (4), the condensate temperature is 30°C, and after condensation, a third mixed gas and a second sieve mixed liquid are obtained; S5. The second sieve mixed liquid is sent to the stabilization tower (5) and distilled to obtain butyraldehyde solution, the second batch of catalyst solution and the third mixed gas.

8. The method for separating carbonyl butyraldehyde according to claim 7, characterized in that: The first mixed gas consists of propylene, propane and synthesis gas (7), the second mixed gas consists of propylene, propane and butyraldehyde, and the third mixed gas consists of propylene and propane.

9. The method for separating carbonyl butyraldehyde according to claim 8, characterized in that: The mixed liquid, the primary screened mixed liquid and the secondary screened mixed liquid are all composed of propylene, propane, a catalyst and butyraldehyde.

Images