Three-reactor series-parallel system for carbonyl synthesis of butyraldehyde

Abstract

A three-reactor series-parallel system for carbonyl synthesis of butyraldehyde, wherein the synthesis gas pipeline is connected to the synthesis gas inlet of the first, second and new first reactors, the propylene pipeline is connected to the feed port of the first and new first reactors, the vent port and liquid outlet of the first and new first reactors are respectively connected to the synthesis gas inlet of the second reactor and the feed end of the material cooler through gas phase and liquid phase pipelines, the discharge end of the material cooler is connected to the liquid inlet of the second reactor through the second liquid phase feed pipeline, the reactor connecting pipeline is connected between the second liquid phase feed pipeline and the liquid inlet of the first reactor, and the new first reactor is connected in parallel or in series with the first reactor and then in series with the second reactor, or the new first reactor or the first reactor is connected in series with the second reactor alone. Accordingly, the three-reactor series-parallel system can achieve full load, long cycle and stable operation, and can avoid fluctuations in the subsequent system.

Description

Technical Field

[0001] The utility model relates to the technical field of carbonyl synthesis of butyraldehyde, in particular to a three-reactor series-parallel system for carbonyl synthesis of butyraldehyde. Background Art

[0002] In the process production of carbonyl synthesis of butyraldehyde, whether the reactor can operate normally directly affects the size of the system load and whether it will cause large fluctuations in the rear system. According to the patent document of the single and double reactor system of carbonyl synthesis of butyraldehyde with the announcement number CN214400308U, it is recorded in the specification that the leakage of the stirrer seal of the reactor will cause the reactor to be cut out for maintenance, so that the system is reduced in quantity and the system is running, and the problem of large fluctuations in the rear system is caused. In addition, considering that the activity of the catalyst is different at different times, the conversion rate of the system is also different at different times, especially the catalyst will cause a large increase in product by-products due to the reduced activity in the later catalytic reaction. Therefore, how to solve the problem that the system load is reduced due to abnormal maintenance of the reactor and the rear system fluctuates greatly, the product output is reduced, and the material consumption is increased, and the problem that the catalyst reduces the activity in the later reaction so that the product by-products increase in large quantities has become one of the important technical problems that technicians in this field need to solve. Utility Model Content

[0003] In order to solve the above technical problems, the present technical scheme adopts the method of adding a new No. 1 reactor. On the one hand, it increases the reaction residence time of the materials to improve the reaction conversion rate, thereby solving the problem of the increase of product by-products due to the decrease in activity of the catalyst in the later stage; on the other hand, it can solve the problem of the reduction of system load due to abnormal maintenance of the reactor, resulting in large fluctuations in the subsequent system, reduced product output and increased material consumption.

[0004] To this end, the present technical scheme provides a three-reactor series-parallel system for carbonyl synthesis of butyraldehyde, which includes: a synthesis gas pipeline, a propylene pipeline, a No. 1 reactor, a No. 2 reactor, a No. 1 gas phase pipeline, a No. 1 liquid phase pipeline, a material cooler, a No. 2 liquid phase feed pipeline, a new No. 1 reactor, a new No. 1 gas phase pipeline, a new No. 1 liquid phase pipeline and a reactor connecting pipeline, wherein the synthesis gas pipeline is respectively connected to the synthesis gas inlet of the No. 1 reactor, the No. 2 reactor and the new No. 1 reactor, the propylene pipeline is respectively connected to the feed port of the No. 1 reactor and the new No. 1 reactor, the vent port and the liquid outlet of the No. 1 reactor are respectively connected to the synthesis gas inlet of the No. 2 reactor and the feed end of the material cooler through the No. 1 gas phase pipeline and the No. 1 liquid phase pipeline, and the discharge end of the material cooler is connected to the No. 2 liquid phase pipeline. The feed pipeline is connected to the liquid inlet of the No. 2 reactor, the vent and liquid outlet of the new No. 1 reactor are respectively connected to the synthesis gas inlet and the No. 1 liquid phase pipeline of the No. 2 reactor through the new No. 1 gas phase pipeline and the new No. 1 liquid phase pipeline, one end of the reactor connecting pipeline is connected to the No. 2 liquid phase feed pipeline, and the other end of the reactor connecting pipeline is connected to the liquid inlet of the No. 1 reactor. By controlling the flow and on-off of the synthesis gas pipeline, the propylene pipeline, the No. 1 gas phase pipeline, the No. 1 liquid phase pipeline, the No. 2 liquid phase feed pipeline, the new No. 1 gas phase pipeline, the new No. 1 liquid phase pipeline and the reactor connecting pipeline, the new No. 1 reactor is connected in parallel or in series with the No. 1 reactor and then connected in series with the No. 2 reactor, or the new No. 1 reactor or the No. 1 reactor is connected in series with the No. 2 reactor alone. Accordingly, if the activity of the catalyst is better in the initial stage of the reaction, the new reactor No. 1 can be connected in parallel with the reactor No. 1 and then in series with the reactor No. 2 to achieve full load production of the three-reactor series-parallel system, thereby ensuring higher product output and productivity; and when the activity of the catalyst decreases in the middle and late stages of the reaction, the new reactor No. 1 can be connected in series with the reactor No. 1 and then in series with the reactor No. 2, so that the raw synthesis gas and propylene are first input into the new reactor No. 1 for reaction, and then discharged from the liquid outlet of the new reactor No. 1 and then into the reactor No. 1 for further reaction, and then discharged from the liquid outlet of the reactor No. 1 and then into the reactor No. 2, so as to achieve full load production of the three-reactor series-parallel system, thereby ensuring higher product output and productivity; and when the activity of the catalyst decreases in the middle and late stages of the reaction, the new reactor No. 1 can be connected in series with the reactor No. 1 and then into ... This increases the reaction residence time of the material and allows it to be fully catalyzed by the catalyst, thereby not only ensuring a higher reaction efficiency but also reducing the generation of product by-products; and when one of the reactors (the new reactor No. 1 or reactor No. 1) has an abnormal situation and needs to be urgently shut down for maintenance, it can be cut out and shut down online without reducing the load while maintaining stable production, and the other reactor can be connected in series with reactor No. 2 to ensure the normal operation of the three-reactor series-parallel system. Therefore, the three-reactor series-parallel system of the present technical solution has the characteristics of full load, long cycle, and good stability, and can greatly reduce energy and material consumption while avoiding large fluctuations in the subsequent system.

[0005] As another implementation of the technical solution, the synthesis gas pipeline is composed of a first synthesis gas pipeline and a second synthesis gas pipeline, the first synthesis gas pipeline is connected to the synthesis gas inlet of the new No. 1 reactor and the No. 1 reactor respectively through the new No. 1 synthesis gas pipeline and the No. 1 synthesis gas pipeline, and the second synthesis gas pipeline is connected to the synthesis gas inlet of the No. 2 reactor, and the venting port of the No. 1 reactor and the venting port of the new No. 1 reactor are connected to the second synthesis gas pipeline through the No. 1 gas phase pipeline and the new No. 1 gas phase pipeline respectively. In this way, it is ensured that the synthesis gas intake and the exhaust of the venting gas of the new No. 1 and No. 1 reactors do not interfere with each other.

[0006] As another implementation of the technical solution, the propylene pipeline is connected to the feed inlet of the new No. 1 reactor and the feed inlet of the No. 1 reactor respectively through the new No. 1 propylene pipeline and the No. 1 propylene pipeline, thereby ensuring the distribution control of the propylene feed.

[0007] As another implementation of the technical solution, a new No. 1 circulating pump is provided on the new No. 1 liquid phase pipeline, and a No. 1 circulating pump is provided on the No. 1 liquid phase pipeline, and the pump outlet of the new No. 1 circulating pump is connected to the pump outlet of the No. 1 circulating pump through a pipeline and then connected to the feed end of the material cooler through a converging pipeline. In this way, the smoothness of the discharge of the new No. 1 and / or No. 1 reactor to the next process link is ensured.

[0008] As another implementation of the technical solution, a new No. 1 return line is connected between the pump inlet and the pump outlet of the new No. 1 circulation pump, and a No. 1 return line is connected between the pump inlet and the pump outlet of the No. 1 circulation pump. Accordingly, by controlling the flow and on-off of the new No. 1 return line and / or the No. 1 return line, fine-tuning control of the liquid level in the new No. 1 and / or No. 1 reactor can be achieved.

[0009] As another implementation of the technical solution, the three-reactor series-parallel system also includes: a new No. 1 temperature control pipeline and a No. 1 temperature control pipeline, wherein one end of the new No. 1 temperature control pipeline is connected to the No. 2 liquid phase feed pipeline, and the other end of the new No. 1 temperature control pipeline is connected to the feed inlet of the new No. 1 reactor, one end of the No. 1 temperature control pipeline is connected to the new No. 1 temperature control pipeline, and the other end of the No. 1 temperature control pipeline is connected to the feed inlet of the No. 1 reactor. Accordingly, by controlling the flow rate and on-off of the new No. 1 and / or No. 1 temperature control pipeline, the reaction temperature in the new No. 1 and / or No. 1 reactor can be adjusted and controlled, thereby ensuring that the reactor has a higher reaction efficiency.

[0010] As another implementation of the technical solution, the three-reactor series-parallel system also includes: a temperature control coil, a hot flow pipeline, a cold flow pipeline, a No. 1 auxiliary temperature control pipeline and a new No. 1 auxiliary temperature control pipeline, wherein the temperature control coil is wound around the No. 2 reactor, one end of the hot flow pipeline is connected to the confluence pipeline, one end of the cold flow pipeline is connected to the new No. 1 temperature control pipeline, the other end of the hot flow pipeline and the other end of the cold flow pipeline are both connected to the inlet end of the temperature control coil, one end of the No. 1 auxiliary temperature control pipeline is connected to the outflow end of the temperature control coil, the other end of the No. 1 auxiliary temperature control pipeline is connected to the feed inlet of the No. 1 reactor, one end of the new No. 1 auxiliary temperature control pipeline is connected to the No. 1 auxiliary temperature control pipeline, and the other end of the new No. 1 auxiliary temperature control pipeline is connected to the new No. 1 temperature control pipeline. Accordingly, the reaction temperature in reactor No. 2 can be adjusted and controlled by setting the temperature control coil, thereby ensuring a higher reaction efficiency of the reactor; in addition, the reaction temperature in reactor No. 1 and / or reactor No. 1 can also be auxiliary fine-tuned and controlled through the new reactor No. 1 and / or reactor No. 1 auxiliary temperature control pipeline.

[0011] As another implementation of the technical solution, a new No. 1 synthesis gas pipeline, a No. 1 synthesis gas pipeline, the starting section of the second synthesis gas pipeline, a new No. 1 propylene pipeline, a No. 1 propylene pipeline, a No. 1 gas phase pipeline, a No. 2 liquid phase feed pipeline, a new No. 1 gas phase pipeline, a pipeline from the outlet of the new No. 1 circulation pump to the outlet of the No. 1 circulation pump, a new No. 1 reflux pipeline, a No. 1 reflux pipeline, a new No. 1 temperature control pipeline, a No. 1 temperature control pipeline, a hot flow pipeline, a cold flow pipeline and a No. 1 auxiliary temperature control pipeline. The pipelines are respectively provided with flow regulating valves and cut-off valves, the reactor connecting pipeline is provided with a cut-off valve, one end of the new No. 1 auxiliary temperature regulating pipeline is connected to the pipe section between the flow regulating valve and the cut-off valve on the No. 1 auxiliary temperature regulating pipeline and the outflow end of the temperature regulating coil, and the other end of the new No. 1 auxiliary temperature regulating pipeline is connected to the pipe section between the flow regulating valve and the cut-off valve on the new No. 1 temperature regulating pipeline and the No. 2 liquid phase feed pipeline, and the new No. 1 auxiliary temperature regulating pipeline is provided with a cut-off valve. Accordingly, by controlling the above-mentioned flow regulating valve and the cut-off valve, the flow and on-off control of the corresponding pipeline can be realized.

[0012] As another implementation of the technical solution, the three-reactor series-parallel system further includes: a vent cooler and a flare, the vent port and the feed port of the No. 2 reactor are respectively connected to the feed end of the vent cooler through pipelines, and the discharge end of the vent cooler is connected to the flare. Accordingly, after the vent air of the No. 2 reactor is cooled by the vent cooler, the vapor material therein can be condensed into liquid material and refluxed into the No. 2 reactor through the feed port, thereby effectively avoiding the waste of materials.

[0013] As another implementation of the technical solution, the No. 1, No. 2 and new No. 1 reactors are all equipped with CO far-infrared online analysis and propylene propane chromatographic online analysis instruments for exhaust air. Based on this, the online real-time monitoring of the three reactor series-parallel system is realized, so that the operation adjustment can be made in time, thereby ensuring the stable operation of the process production. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 The utility model is a structural connection diagram of a three-reactor series-parallel system for carbonyl synthesis of butyraldehyde.

[0015] Explanation of symbols in the accompanying drawings:

[0016] R101 Reactor No. 1; R102 Reactor No. 2; T102 Temperature control coil; R101A New Reactor No. 1; 1A First Synthesis Gas Pipeline; 1A1 New Synthesis Gas Pipeline No. 1; 1A2 Synthesis Gas Pipeline No. 1; 1B Second Synthesis Gas Pipeline; 2A New Propylene Pipeline No. 1; 2B Propylene Pipeline No. 1; 3 Gas Pipeline No. 1; 4 Liquid Pipeline No. 1; 4A Converging Pipeline; E101 Material Cooler; 5 Liquid Feed Pipeline No. 2; 6 New Gas Pipeline No. 1; 7 New Liquid Pipeline No. 1; 7A Pipeline; 8 Reactor Connecting Pipeline; 9 Discharge Pipeline; P101C New Circulation Pump No. 1; P101B Circulation Pump No. 1; 10 New Reflux Pipeline No. 1; 11 Reflux Pipeline No. 1; 12 New Temperature Control Pipeline No. 1; 13 Temperature Control Pipeline No. 1; 14 Hot flow pipeline; 15 cold flow pipeline; 16 No. 1 auxiliary temperature control pipeline; 17 New No. 1 auxiliary temperature control pipeline; FV1201A, FV1201, FV1301, FV1205A, FV1205, PV1202, LV1201, PV1202A, LV1201A, FV1203A, FV1203, TV1201A, TV1201, TV1209A, TV1209B, FV1206 flow regulating valve and shut-off valve; V1201, V1202 shut-off valves; E102 vent cooler. DETAILED DESCRIPTION

[0017] The detailed description and technical contents of the present invention are described below with reference to the accompanying drawings. However, the accompanying drawings are only provided for reference and description and are not intended to limit the present invention.

[0018] In the context of this specification, any two or more embodiments of the present invention may be arbitrarily combined, and the technical solutions thus formed still belong to part of the original disclosure of this specification and also fall within the protection scope of the present invention.

[0019] like Figure 1As shown, a specific embodiment of a three-reactor series-parallel system for carbonyl synthesis of butyraldehyde of the utility model is shown. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde (hereinafter referred to as the three-reactor series-parallel system) includes a synthesis gas pipeline, a propylene pipeline, a No. 1 reactor R101, a No. 2 reactor R102, a No. 1 gas phase pipeline 3, a No. 1 liquid phase pipeline 4, a material cooler E101, a No. 2 liquid phase feed pipeline 5, a new No. 1 reactor R101A, a new No. 1 gas phase pipeline 6, a new No. 1 liquid phase pipeline 7 and a reactor connecting pipeline 8. Among them, the synthesis gas pipeline is respectively connected to the synthesis gas inlet of the No. 1 reactor R101, the No. 2 reactor R102 and the new No. 1 reactor R101A. The propylene pipeline is respectively connected to the feed inlet of the No. 1 reactor R101 and the new No. 1 reactor R101A. The vent and liquid outlet of the No. 1 reactor R101 are connected to the synthesis gas inlet of the No. 2 reactor R102 and the feed end of the material cooler E101 through the No. 1 gas phase pipeline 3 and the No. 1 liquid phase pipeline 4 respectively. The discharge end of the material cooler E101 is connected to the liquid inlet of the No. 2 reactor R102 through the No. 2 liquid phase feed pipeline 5. The material cooler E101 is the main component for adjusting the reaction temperature of the No. 1, No. 2 and new No. 1 reactors R101, R102, R101A. The vent and liquid outlet of the new No. 1 reactor R101A are connected to the synthesis gas inlet of the No. 2 reactor R102 and the No. 1 liquid phase pipeline 4 respectively through the new No. 1 gas phase pipeline 6 and the new No. 1 liquid phase pipeline 7. One end of the reactor connection pipeline 8 is connected to the No. 2 liquid phase feed pipeline 5, and the other end of the reactor connection pipeline 8 is connected to the liquid inlet of the No. 1 reactor R101. By controlling the flow and on-off of the synthesis gas pipeline, propylene pipeline, No. 1 gas phase pipeline 3, No. 1 liquid phase pipeline 4, No. 2 liquid phase feed pipeline 5, new No. 1 gas phase pipeline 6, new No. 1 liquid phase pipeline 7 and the reactor connection pipeline 8, the new No. 1 reactor R101A is connected in parallel or in series with the No. 1 reactor R101 and then connected in series with the No. 2 reactor R102, or the new No. 1 reactor R101A or the No. 1 reactor R101 is connected in series with the No. 2 reactor R102 alone. In addition, the liquid outlet of the No. 2 reactor R102 can also be connected to the high and low temperature evaporator (not shown) through the discharge pipeline 9 to perform the discharge operation.

[0020] More specifically, in this embodiment, the synthesis gas pipeline is composed of a first synthesis gas pipeline 1A and a second synthesis gas pipeline 1B. The first synthesis gas pipeline 1A is connected to the synthesis gas inlet of the new No. 1 reactor R101A and the No. 1 reactor R101 through the new No. 1 synthesis gas pipeline 1A1 and the No. 1 synthesis gas pipeline 1A2 respectively. The second synthesis gas pipeline 1B is connected to the synthesis gas inlet of the No. 2 reactor R102, and the venting port of the No. 1 reactor R101 and the venting port of the new No. 1 reactor R101A are connected to the second synthesis gas pipeline 1B through the No. 1 gas phase pipeline 3 and the new No. 1 gas phase pipeline 6 respectively, so as to ensure that the synthesis gas intake and the exhaust of the new No. 1 and No. 1 reactors R101A and R101 do not interfere with each other. In addition, the propylene pipeline is connected to the feed inlet of the new No. 1 reactor R101A and the feed inlet of the No. 1 reactor R101 through the new No. 1 propylene pipeline 2A and the No. 1 propylene pipeline 2B respectively, so as to ensure the distribution control of the propylene feed. In addition, a new No. 1 circulation pump P101C can be arranged on the new No. 1 liquid phase pipeline 7, and a No. 1 circulation pump P101B can be arranged on the No. 1 liquid phase pipeline 4, and the pump outlet of the new No. 1 circulation pump P101C is connected to the pump outlet of the No. 1 circulation pump P101B through the pipeline 7A and then connected to the feed inlet of the material cooler E101 through the converging pipeline 4A, so as to ensure the smoothness of the discharge of the new No. 1 and / or No. 1 reactors R101A, R101 to the next process link. In addition, a new No. 1 reflux pipeline 10 can be connected between the pump inlet and pump outlet of the new No. 1 circulation pump P101C, and a No. 1 reflux pipeline 11 can be connected between the pump inlet and pump outlet of the No. 1 circulation pump P101B. By controlling the flow and on-off of the new No. 1 reflux pipeline 10 and / or the No. 1 reflux pipeline 11, fine-tuning control of the liquid level in the new No. 1 and / or No. 1 reactors R101A, R101 can be achieved.

[0021] Furthermore, the three-reactor series-parallel system may also include a new No. 1 temperature control pipeline 12 and a No. 1 temperature control pipeline 13. Among them, one end of the new No. 1 temperature control pipeline 12 is connected to the No. 2 liquid phase feed pipeline 5, and the other end of the new No. 1 temperature control pipeline 12 is connected to the feed inlet of the new No. 1 reactor R101A. One end of the No. 1 temperature control pipeline 13 is connected to the new No. 1 temperature control pipeline 12, and the other end of the No. 1 temperature control pipeline 13 is connected to the feed inlet of the No. 1 reactor R101. By controlling the flow rate and on-off of the new No. 1 and / or No. 1 temperature control pipelines 12 and 13, the reaction temperature in the new No. 1 and / or No. 1 reactors R101A and R101 can be adjusted and controlled, thereby ensuring that the reactors have a higher reaction efficiency.

[0022] Furthermore, the three-reactor series-parallel system may also include a temperature control coil T102, a hot flow pipeline 14, a cold flow pipeline 15, a No. 1 auxiliary temperature control pipeline 16 and a new No. 1 auxiliary temperature control pipeline 17. Among them, the temperature control coil T102 is wound around the No. 2 reactor. One end of the hot flow pipeline 14 is connected to the converging pipeline 4A, one end of the cold flow pipeline 15 is connected to the new No. 1 temperature control pipeline 12, and the other end of the hot flow pipeline 14 and the other end of the cold flow pipeline 15 are both connected to the inflow end of the temperature control coil T102. One end of the No. 1 auxiliary temperature control pipeline 16 is connected to the outflow end of the temperature control coil T102, and the other end of the No. 1 auxiliary temperature control pipeline 16 is connected to the feed inlet of the No. 1 reactor R101. One end of the new No. 1 auxiliary temperature control pipeline 17 is connected to the No. 1 auxiliary temperature control pipeline 16, and the other end of the new No. 1 auxiliary temperature control pipeline 17 is connected to the new No. 1 temperature control pipeline 12. The temperature control coil T102 can be used to adjust and control the reaction temperature in the No. 2 reactor R102, thereby ensuring a higher reaction efficiency of the reactor. In addition, the reaction temperature in the new No. 1 and / or No. 1 reactors R101A, R101 can also be assisted in fine-tuning control through the new No. 1 and / or No. 1 auxiliary temperature control pipelines 17, 16.

[0023] Furthermore, in the new No. 1 synthesis gas pipeline, the No. 1 synthesis gas pipeline, the starting section of the second synthesis gas pipeline, the new No. 1 propylene pipeline, the No. 1 propylene pipeline, the No. 1 gas phase pipeline, the No. 2 liquid phase feed pipeline, the new No. 1 gas phase pipeline, the pipeline from the outlet of the new No. 1 circulation pump to the outlet of the No. 1 circulation pump, the new No. 1 reflux pipeline, the No. 1 reflux pipeline, the new No. 1 temperature control pipeline, the No. 1 temperature control pipeline, the hot flow pipeline, the cold flow pipeline and the No. 1 auxiliary pipeline, the No. 1 reflux pipeline, the No. 1 temperature control pipeline, the No. 1 temperature control pipeline, the hot flow pipeline, the cold flow pipeline and the No. 1 auxiliary pipeline, the No. 1 reflux pipeline, the No. 1 reflux pipeline, the No. 1 temperature control pipeline, the No. 1 temperature control pipeline, the No. 1 reflux ... The auxiliary temperature adjustment pipeline is respectively provided with flow regulating valves and cut-off valves FV1201A, FV1201, FV1301, FV1205A, FV1205, PV1202, LV1201, PV1202A, LV1201A, FV1203A, FV1203, TV1201A, TV1201, TV1209A, TV1209B, and FV1206. A cut-off valve V1201 is provided on the reactor connecting pipeline 8. One end of the new No. 1 auxiliary thermostatic pipeline 17 is connected to the pipe section between the flow regulating valve and the cut-off valve FV1206 on the No. 1 auxiliary thermostatic pipeline 16 and the outflow end of the thermostatic coil T102, and the other end of the new No. 1 auxiliary thermostatic pipeline 17 is connected to the pipe section between the flow regulating valve and the cut-off valve TV1201A on the new No. 1 thermostatic pipeline 12 and the No. 2 liquid phase feed pipeline 5, and the cut-off valve V1202 is provided on the new No. 1 auxiliary thermostatic pipeline 17. By controlling the above-mentioned flow regulating valve and cut-off valve, the flow and on-off of the corresponding pipeline can be controlled.

[0024] In this embodiment, the three-reactor series-parallel system may also include a vent cooler E102 and a flare (not shown). The vent port and feed port of the No. 2 reactor R102 are respectively connected to the feed end of the vent cooler E102 through pipelines, and the discharge end of the vent cooler E102 is connected to the flare. After the vent air of the No. 2 reactor R102 is cooled by the vent cooler E102, the vapor material therein can be condensed into liquid material and refluxed into the No. 2 reactor R102 through the feed port, so as to effectively avoid the waste of materials.

[0025] In this embodiment, the No. 1, No. 2 and new No. 1 reactors can all be equipped with CO far-infrared online analysis and vented air propylene propane chromatography online analysis instruments (not shown in the figure) to achieve online real-time monitoring of the three-reactor series-parallel system, so as to make timely operation adjustments and ensure the stable operation of the process production.

[0026] When the three-reactor series-parallel system of the utility model is in operation:

[0027] (1) When the catalyst has good initial activity, the new No. 1 reactor R101A can be connected in parallel with the No. 1 reactor R101 and then connected in series with the No. 2 reactor R102 to achieve high-efficiency operation. The main process is as follows: the propylene raw material enters the new No. 1 and No. 1 reactors R101A and R101 through the new No. 1 and No. 1 propylene pipelines 2A and 2B, and at the same time, the raw material synthesis gas enters the new No. 1 and No. 1 reactors R101A and R101 through the new No. 1 and No. 1 synthesis gas pipelines 1A1 and 1A2, the reactor connecting pipeline 8 is closed, and the reaction temperature of the new No. 1 and No. 1 reactors R101A and R101 is controlled by adjusting the flow rate and / or the opening and closing of the new No. 1 and / or No. 1 temperature control pipelines 12 and 13. Then, the new No. 1 and No. 1 reactors R101A and R101 send the lower liquid through the new No. 1 and No. 1 liquid phase pipelines 7 and 4 to the No. 2 reactor R102 through the material cooler E101 and the No. 2 liquid phase feed pipeline 5. At the same time, the new No. 1 and No. 1 reactors R101A and R101 send the vented exhaust through the new No. 1 and No. 1 gas phase pipelines 6 and 3 to the No. 2 reactor R102 through the second synthesis gas pipeline 1B mixed with the raw synthesis gas. The reaction temperature of the No. 2 reactor R102 is controlled by controlling the flow and / or on-off of the hot flow and / or cold flow pipelines 14 and 15 and the outflow end of the temperature regulating coil T102. After the reaction of the No. 2 reactor R102 is completed, the material is discharged and vented.

[0028] (2) When the activity of the catalyst decreases in the middle and late stages of the reaction, the reaction time of the materials in the reactor can be increased by connecting the new No. 1 reactor R101A in series with the No. 1 reactor R101 first and then with the No. 2 reactor R102 in series, thereby reducing the generation of product by-products and ensuring a high production efficiency. The main process is: open the new No. 1 propylene pipeline 2A and the new No. 1 synthesis gas pipeline 1A1, close the No. 1 propylene pipeline 2B, and because the main reaction of the series connection occurs in the new No. 1 reactor R101A, the flow of the No. 1 synthesis gas pipeline 1A2 is reduced so that the propylene raw material and the raw synthesis gas enter the new No. 1 reactor R101A, and a small part of the raw synthesis gas enters the No. 1 reactor R101. During the reaction, the liquid level of the new No. 1 reactor R101A is mainly controlled by adjusting the flow of the new No. 1 liquid phase pipeline 7, and the reaction temperature of the new No. 1 reactor R101A is mainly controlled by adjusting the flow and / or on-off control of the new No. 1 temperature control pipeline 12. Open the reactor connecting pipeline 8, and the new reactor No. 1 R101A sends the lower liquid into the reactor No. 1 R101 through the new No. 1 liquid phase pipeline 7 via the material cooler E101 and the reactor connecting pipeline 8. The reaction temperature of the reactor No. 1 R101 is mainly controlled by adjusting the flow rate and / or on-off of the No. 1 temperature control pipeline 13. After the reaction of the No. 1 reactor R101, the lower liquid is sent to the No. 2 reactor R102 through the No. 1 liquid phase pipeline 4 through the material cooler E101 and the No. 2 liquid phase feed pipeline 5, and the new No. 1 and No. 1 reactors R101A and R101 are vented and exhausted through the new No. 1 and No. 1 gas phase pipelines 6 and 3 through the second synthesis gas pipeline 1B and mixed with the raw synthesis gas to be sent to the No. 2 reactor R102. At the same time, the reaction temperature of the No. 2 reactor R102 is controlled by controlling the flow rate and / or on-off of the hot flow and / or cold flow pipelines 14 and 15 and the outflow end of the temperature regulating coil T102. After the reaction of the No. 2 reactor R102 is completed, the material is discharged and vented.

[0029] (3) When an abnormal situation occurs in the new reactor No. 1 and it needs to be shut down for emergency maintenance, the new propylene pipeline No. 1 2A, the new synthesis gas pipeline No. 1 1A1, the reactor connecting pipeline 8, the new gas phase pipeline No. 1 6, the new liquid phase pipeline No. 1 7, the new temperature control pipeline No. 12 and the new auxiliary temperature control pipeline No. 17 connected to the new reactor No. 1 R101A are closed, so that the reactor No. 1 R101 and the reactor No. 2 R102 are connected in series for operation.

[0030] (4) When an abnormal situation occurs in the No. 1 reactor and it needs to be shut down for emergency maintenance, the No. 1 propylene pipeline 2B, No. 1 synthesis gas pipeline 1A2, reactor connecting pipeline 8, No. 1 gas phase pipeline 3, No. 1 liquid phase pipeline 4, No. 1 temperature control pipeline 13 and No. 1 auxiliary temperature control pipeline 16 connected to the No. 1 reactor R101 are closed, so that the new No. 1 reactor R101A is connected in series with the No. 2 reactor R102 for operation.

[0031] In summary, the three-reactor series-parallel system for carbonyl synthesis of butyraldehyde using the utility model, if the activity of the catalyst is better in the initial stage of the reaction, the new reactor No. 1 can be connected in parallel with the reactor No. 1 and then connected in series with the reactor No. 2 to achieve full load production of the three-reactor series-parallel system, thereby ensuring higher product output and productivity; and when the activity of the catalyst decreases in the middle and late stages of the reaction, the new reactor No. 1 can be connected in series with the reactor No. 1 and then connected in series with the reactor No. 2, so that the raw material synthesis gas and propylene are first input into the new reactor No. 1 for reaction, and then the material is discharged from the liquid outlet of the new reactor No. 1 and then enters the reactor No. 1 for continued reaction, and then the reactor No. 1 is connected in series with the reactor No. 2. The material discharged from the liquid outlet enters the No. 2 reactor, thereby increasing the reaction residence time of the material and being fully catalyzed by the catalyst, thereby not only ensuring a high reaction efficiency, but also reducing the generation of product by-products; and when one of the reactors (the new No. 1 reactor or the No. 1 reactor) has an abnormal situation and needs to be urgently shut down for maintenance, it can be cut off and shut down online without reducing the load while maintaining stable production, and the other reactor can be connected in series with the No. 2 reactor to ensure the normal operation of the three-reactor series-parallel system. Therefore, the three-reactor series-parallel system of the present technical solution has the characteristics of full load, long cycle, and good stability, and can greatly reduce the consumption of energy and materials while avoiding large fluctuations in the subsequent system.

[0032] The above are only preferred embodiments of the present invention and are not intended to limit the patent scope of the present invention. Other equivalent changes made using the patent concept of the present invention should all fall within the patent protection scope of the present invention.

Claims

1. A three-reactor series-parallel system for carbonyl synthesis of butyraldehyde, comprising: A syngas pipeline, a propylene pipeline, a No. 1 reactor, a No. 2 reactor, a No. 1 gas phase pipeline, a No. 1 liquid phase pipeline, a material cooler and a No. 2 liquid phase feed pipeline, wherein the syngas pipeline is respectively connected to the syngas inlets of the No. 1 reactor and the No. 2 reactor, the propylene pipeline is connected to the feed port of the No. 1 reactor, the venting port and the liquid outlet of the No. 1 reactor are respectively connected to the syngas inlet of the No. 2 reactor and the feed end of the material cooler through the No. 1 gas phase pipeline and the No. 1 liquid phase pipeline, and the discharge end of the material cooler is connected to the liquid inlet of the No. 2 reactor through the No. 2 liquid phase feed pipeline; characterized in that it also includes: a new No. 1 reactor, a new No. 1 gas phase pipeline, a new No. 1 liquid phase pipeline and a reactor connecting pipeline, the syngas pipeline and the propylene pipeline are also respectively connected to the The syngas inlet and the feed inlet are connected, the venting port and the liquid outlet of the new reactor No. 1 are connected to the syngas inlet of the reactor No. 2 and the liquid phase pipeline No. 1 respectively through the new gas phase pipeline No. 1 and the new liquid phase pipeline No. 1, one end of the reactor connecting pipeline is connected to the liquid phase feed pipeline No. 2, and the other end of the reactor connecting pipeline is connected to the liquid inlet of the reactor No. 1, and the flow and on-off control of the syngas pipeline, propylene pipeline, No. 1 gas phase pipeline, No. 1 liquid phase pipeline, No. 2 liquid phase feed pipeline, new No. 1 gas phase pipeline, new No. 1 liquid phase pipeline and reactor connecting pipeline can be controlled so that the new reactor No. 1 is connected in parallel or in series with the reactor No. 1 and then connected in series with the reactor No. 2, or the new reactor No. 1 or the reactor No. 1 is connected in series with the reactor No. 2 alone.

2. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 1, characterized in that: The synthesis gas pipeline is composed of a first synthesis gas pipeline and a second synthesis gas pipeline. The first synthesis gas pipeline is connected to the synthesis gas inlets of the new No. 1 reactor and the No. 1 reactor respectively through the new No. 1 synthesis gas pipeline and the No. 1 synthesis gas pipeline which are separately set up. The second synthesis gas pipeline is connected to the synthesis gas inlet of the No. 2 reactor. The vent of the No. 1 reactor and the vent of the new No. 1 reactor are connected to the second synthesis gas pipeline respectively through the No. 1 gas phase pipeline and the new No. 1 gas phase pipeline.

3. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 2, characterized in that: The propylene pipeline is connected to the feed inlet of the new No. 1 reactor and the feed inlet of the No. 1 reactor respectively through the new No. 1 propylene pipeline and the No. 1 propylene pipeline which are separately provided.

4. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 3, characterized in that: A new No. 1 circulation pump is arranged on the new No. 1 liquid phase pipeline, and a No. 1 circulation pump is arranged on the No. 1 liquid phase pipeline. The pump outlet of the new No. 1 circulation pump is connected to the pump outlet of the No. 1 circulation pump through a pipeline and then connected to the feed end of the material cooler through a converging pipeline.

5. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 4, characterized in that: A new No. 1 return pipeline is connected between the pump inlet and the pump outlet of the new No. 1 circulation pump, and a No. 1 return pipeline is connected between the pump inlet and the pump outlet of the No. 1 circulation pump.

6. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 5, characterized in that: Also includes: A new No. 1 temperature control pipeline and a No. 1 temperature control pipeline, one end of the new No. 1 temperature control pipeline is connected to the No. 2 liquid phase feed pipeline, and the other end of the new No. 1 temperature control pipeline is connected to the feed inlet of the new No. 1 reactor, one end of the No. 1 temperature control pipeline is connected to the new No. 1 temperature control pipeline, and the other end of the No. 1 temperature control pipeline is connected to the feed inlet of the No. 1 reactor.

7. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 6, characterized in that: Also includes: A temperature controlling coil, a hot flow pipeline, a cold flow pipeline, a No. 1 auxiliary temperature controlling pipeline and a new No. 1 auxiliary temperature controlling pipeline, wherein the temperature controlling coil is wound around the No. 2 reactor, one end of the hot flow pipeline is connected to the confluence pipeline, one end of the cold flow pipeline is connected to the new No. 1 temperature controlling pipeline, the other end of the hot flow pipeline and the other end of the cold flow pipeline are both connected to the inlet end of the temperature controlling coil, one end of the No. 1 auxiliary temperature controlling pipeline is connected to the outflow end of the temperature controlling coil, the other end of the No. 1 auxiliary temperature controlling pipeline is connected to the feed inlet of the No. 1 reactor, one end of the new No. 1 auxiliary temperature controlling pipeline is connected to the No. 1 auxiliary temperature controlling pipeline, and the other end of the new No. 1 auxiliary temperature controlling pipeline is connected to the new No. 1 temperature controlling pipeline.

8. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 7, characterized in that: The new No. 1 synthesis gas pipeline, the No. 1 synthesis gas pipeline, the starting section of the second synthesis gas pipeline, the new No. 1 propylene pipeline, the No. 1 propylene pipeline, the No. 1 gas phase pipeline, the No. 2 liquid phase feed pipeline, the new No. 1 gas phase pipeline, the pipeline from the pump outlet of the new No. 1 circulation pump to the pump outlet of the No. 1 circulation pump, the new No. 1 reflux pipeline, the No. 1 reflux pipeline, the new No. 1 temperature control pipeline, the No. 1 temperature control pipeline, the hot flow pipeline, the cold flow pipeline and the No. 1 auxiliary temperature control pipeline are respectively provided with flow regulating valves. and a cut-off valve, the reactor connecting pipeline is provided with a cut-off valve, one end of the new No. 1 auxiliary temperature control pipeline is connected to the pipe section between the flow regulating valve and the cut-off valve on the No. 1 auxiliary temperature control pipeline and the outflow end of the temperature control coil, the other end of the new No. 1 auxiliary temperature control pipeline is connected to the pipe section between the flow regulating valve and the cut-off valve on the new No. 1 temperature control pipeline and the No. 2 liquid phase feed pipeline, and a cut-off valve is provided on the new No. 1 auxiliary temperature control pipeline.

9. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 1, characterized in that: Also includes: A vent cooler and a flare, wherein the vent port and the feed port of the No. 2 reactor are respectively connected to the feed end of the vent cooler through pipelines, and the discharge end of the vent cooler is connected to the flare.

10. The three-reactor series-parallel system for carbonyl synthesis of butyraldehyde according to claim 1, characterized in that: The No. 1, No. 2 and new No. 1 reactors are all equipped with CO far-infrared online analysis and vented air propylene propane chromatography online analysis instruments.

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