Nonene production system and automatic switching method thereof

Abstract

The invention discloses a nonene production system and an automatic switching method thereof, and relates to the technical field of nonene production processes, the system comprises at least three nonene reactors connected in parallel, at least one of the nonene reactors is used as a standby reactor, and the rest is a running reactor; a feed port is formed in the top of each nonene reactor, and a liquid phase discharge port is formed in the bottom of each nonene reactor; all-component online analyzers are arranged at the bottom liquid phase discharge holes; a feeding hole in the top of each nonene reactor is respectively connected with a feeding pipeline and an oil gas recovery pipeline, and a liquid-phase discharging hole in the bottom of each nonene reactor is respectively connected with a discharging pipeline and a liquid-phase recovery pipeline; a feeding pipeline, an oil gas recovery pipeline, a discharging pipeline and a liquid phase recovery pipeline of each nonene reactor are respectively provided with a valve, and each nonene reactor is provided with a preheating device. The switching of the parallel reactors and the switching of the heating heat exchangers can be quickly realized through a one-key switching program in an automatic control mode.

Description

Technical Field

[0001] The present invention relates to the technical field of nonene production technology, and more particularly to a nonene production system and an automatic switching method thereof. Background Art

[0002] In the current production process of nonene, two nonene reactors are used and one is used as a spare. Since the catalyst in the nonene reactor has a short life, the catalyst needs to be replaced every three months. When the reactor is shut down for maintenance and catalyst replacement, the valve needs to be manually switched, which has the risk of human error, poor safety and reliability, low work efficiency, and heavy workload. Summary of the invention

[0003] In order to solve the problems existing in the prior art, the present invention provides a nonene production system and an automatic switching method thereof. The present invention provides a method for automatically switching a nonene reactor, which can realize one-key automatic switching, complete the functions of stopping the reactor, recycling residual materials, and switching on the heater, without manual operation, greatly reducing the risks caused thereby.

[0004] One of the objects of the present invention is to provide a nonene production system.

[0005] The nonene production system of the present invention comprises:

[0006] At least three nonene reactors connected in parallel, at least one of which is used as a standby reactor and the rest are operating reactors;

[0007] Each of the nonene reactors is provided with a feed port at the top and a liquid phase discharge port at the bottom; a full-component online analyzer is provided at the bottom liquid phase discharge port; the feed port at the top of each nonene reactor is respectively connected to the feed pipeline and the oil and gas recovery pipeline, and the liquid phase discharge port at the bottom of each nonene reactor is respectively connected to the discharge pipeline and the liquid phase recovery pipeline; valves are respectively installed on the feed pipeline, oil and gas recovery pipeline, discharge pipeline and liquid phase recovery pipeline of each nonene reactor, and each nonene reactor is equipped with a preheating device.

[0008] Preferably,

[0009] The preheating device comprises: a steam drum and a heat exchanger;

[0010] The steam drum is connected with the shell side of the nonene reactor through a preheating pipe, and the heat exchanger is connected in parallel to the preheating pipe.

[0011] Preferably,

[0012] Heat exchange valves are installed on both sides of the heat exchanger, and a temperature indicating controller is arranged at the outlet end of the heat exchanger, and the temperature indicating controller is electrically connected to the heat exchange valve.

[0013] Preferably,

[0014] The steam drum is provided with a steam recovery pipeline; and / or,

[0015] A temperature detector is provided on the shell side of each nonene reactor.

[0016] Preferably,

[0017] The system is provided with an automatic control unit, which comprises a data acquisition module, a data processing module and a control module which are connected in sequence.

[0018] The present invention can configure the operation station and engineer station of the DCS system during the actual operation process. Each group of operation stations / engineer stations is based on industrial standard PC hardware and is set in the central control room or the on-site cabinet room to display operation data and start debugging and maintenance for on-site operators. The DCS system completes process control, operation, monitoring and management, and completes some advanced process control strategies. The DCS system has hardware redundancy configurations such as the central processing unit (CPU), control I / O card, power supply unit, and communication system. The DCS system can communicate data with the SIS system, process computer system, and MCC. The communication bus is redundant, the communication protocol is standardized, and it can support communication networks worldwide.

[0019] Preferably,

[0020] The data acquisition module is electrically connected to the full-component online analyzer of each nonene reactor; the data acquisition module is electrically connected to the temperature detector on the shell side of each nonene reactor;

[0021] The control module is electrically connected to the valves on the feed pipeline, oil and gas recovery pipeline, discharge pipeline and liquid phase recovery pipeline of each nonene reactor respectively; the control module is electrically connected to the heat exchange valve of each nonene reactor respectively.

[0022] Preferably,

[0023] A lower head filter is arranged in the lower head of each nonene reactor, the upper part of the lower head filter is a conical structure which is narrow at the top and wide at the bottom, the side wall of the conical structure is a closed smooth inclined surface, the lower part of the lower head filter is a columnar structure, the side wall and the bottom of the columnar structure are both filter structures, a through hole is arranged at the bottom of the columnar structure, a drainage pipe is connected downwardly to the through hole, a material outlet is arranged at the bottom of the lower head in the nonene reactor, and the drainage pipe of the lower head filter is arranged above the material outlet at the bottom of the nonene reactor and is connected thereto.

[0024] Preferably,

[0025] The bottom edge of the conical structure is consistent in shape with the top edge of the columnar structure and is connected; and / or,

[0026] The conical structure is a cone or a frustum; preferably, a cone, a pyramid, a truncated cone or a prism; and / or,

[0027] The columnar structure is a cylinder or a prism; and / or,

[0028] The slope angle of the smooth slope is greater than or equal to the sliding angle of the catalyst, preferably 40° to 55°; and / or,

[0029] The filter structure is a wire mesh, and / or the mesh number of the filter structure is 100 to 800 meshes, preferably 200 to 800 meshes; and / or,

[0030] The nominal diameter of the draft tube matches the material outlet of the nonene reactor; and / or,

[0031] The height of the drainage tube is 500 mm to 800 mm.

[0032] Preferably,

[0033] The bottom diameter of the cone-shaped structure is 800-1200 mm; preferably, when the cone-shaped structure is a pyramid or a prism, the bottom area of ​​the cone-shaped structure is 0.5 m 2 ~1.2m 2 and / or,

[0034] The lower head filter screen is made of 321 stainless steel or titanium alloy; and / or,

[0035] The total height of the lower head filter is 1300mm-1700mm; and / or,

[0036] The height of the columnar structure is 200 to 400 mm; and / or,

[0037] A discharge port is provided at the bottom of the nonene reactor; preferably, the discharge port is arranged beside the material outlet; more preferably, the nominal diameter of the discharge port is 150-250 mm.

[0038] The present invention adopts a method of adding a lower head filter screen at the lower head of the nonene reactor. The upper part of the lower head filter screen structure is a smooth plane with a certain slope, which is convenient for the top catalyst residue to be scattered to the bottom when it falls, avoiding the accumulation of residue in the circulation area to cause blockage, and reducing the cleaning frequency of the lower head filter screen. The present invention collects the residues dropped during the long-term operation of the nonene reactor, so that the residues are concentrated in the lower part of the lower head of the reactor and the lower head filter screen structure, which is convenient for the operator to perform a one-time cleaning when the reactor is switched, and avoids frequent cleaning of the coalescer water phase shear regulating valve A during the production operation of the device. In addition, the medium of the downstream heat exchanger can be made cleaner, the fouling coefficient can be reduced when designing the heat exchanger, the heat transfer coefficient becomes larger, the heat exchange area is reduced, and the heat exchanger footprint is reduced, thereby saving space; after the reaction product passes through the lower head filter screen, the abrasiveness of the medium is greatly reduced, and the abrasion of the internal parts of the coalescer is reduced, which is conducive to extending the life of the internal parts of the coalescer. In summary, the lower head filter screen of the present invention helps to meet process requirements and improve the stability of device operation.

[0039] A second object of the present invention is to provide an automatic switching method for a nonene production system.

[0040] The automatic switching method of the nonene production system of the present invention is characterized in that the method comprises:

[0041] The automatic control unit compares the propylene conversion rate sent by the full-component online analyzer with the set value. If the propylene conversion rate is less than the set value, the control system enters the reactor switching program; specifically, the online analyzer sends the propylene conversion rate to the data acquisition module, the data acquisition module sends the data to the data processing module, the data processing module compares, if the propylene conversion rate is less than the set value, the data processing module notifies the control module control system to perform the reactor switching program;

[0042] The reactor switching procedure includes:

[0043] After the preheating device of the standby reactor is turned on for preheating, the valves on the feed pipe and the discharge pipe of the standby reactor are opened, and the standby reactor is switched to the operating reactor;

[0044] At the same time, the valves on the feed pipe and discharge pipe of the operating reactor whose propylene conversion rate is less than the set value are closed, and the valve on the liquid phase recovery pipe of its oil and gas recovery pipe is opened. At this time, the operating reactor is switched to the standby reactor.

[0045] Preferably,

[0046] After the preheating device of the standby reactor is opened for preheating, the operation of opening the valves on the feed pipe and the discharge pipe of the standby reactor comprises:

[0047] The preheating device of the standby reactor is turned on for preheating, and the automatic control unit compares the temperature sent by the temperature detector with the set temperature. When the temperature is the same as the set temperature, the automatic control unit gradually increases the opening of the valves on the feed pipe and the discharge pipe of the standby reactor until they are fully opened;

[0048] The operation of closing the valves on the feed pipe and the discharge pipe of the operating reactor whose propylene conversion rate is less than the set value includes:

[0049] The automatic control unit gradually reduces the opening of the valves on the feed pipe and the discharge pipe of the operating reactor whose propylene conversion rate is less than the set value to fully close, and opens the valve on the liquid phase recovery pipe of its oil and gas recovery pipe.

[0050] Preferably,

[0051] The set value of the propylene conversion rate is 50%-60%, preferably 55%-60%; and / or,

[0052] The preheating setting temperature is 80-150° C.; and / or,

[0053] The valve is gradually adjusted up and down at the same rate, preferably 25-50% / h, so as to ensure that the sum of feeds remains unchanged during the reactor switching process and does not affect the load of downstream equipment; and / or,

[0054] The valves on the feed pipeline, oil and gas recovery pipeline, discharge pipeline and liquid recovery pipeline of each nonene reactor and the heat exchange valve of each nonene reactor are delayed interlock valves. Preferably, the delay time is 1 to 5 minutes, and the delay time can be used for judgment by the staff to avoid misoperation.

[0055] Preferably, the starting of the preheating device includes:

[0056] The control module of the automatic control unit opens the heat exchange valve of the preheating device, and the heat exchanger heats the heat exchange medium. After the heat exchange medium in the drum is heated, it enters the shell side of the nonene reactor to preheat the reactor; preferably, the heat exchange medium is water.

[0057] Preferably,

[0058] During the preheating process of the preheating device, the steam flow rate of the heat exchanger is controlled by the controller according to the temperature indicating the outlet of the heat exchanger;

[0059] Preferably,

[0060] When the temperature is higher than 135-145°C, adjust the opening of the heat exchange valve to 5-15%; when the temperature is lower than 85-95°C, adjust the opening of the heat exchange valve to 85-95%.

[0061] Preferably,

[0062] The automatic control unit compares the shell temperature of the nonene reactor sent by the temperature detector with the set temperature. When the temperature is the same as the set temperature, the automatic control unit closes the heat exchange valves on both sides of the heat exchanger. Preferably, the set temperature is 80-150°C.

[0063] The following solutions can be adopted:

[0064] The present invention provides a method for automatically switching parallel reactors, which can realize the switching of at least three parallel reactors and the recovery of residual materials:

[0065] When the nonene reactor A and the nonene reactor B are in normal operation, the nonene reactor A and the nonene reactor B are operating reactors, and the nonene reactor C is a standby reactor. At this time, the valves on the feed pipes and the discharge pipes of the nonene reactor A and the nonene reactor B are in an open state, and the valves on the feed pipes and the discharge pipes of the nonene reactor C are in a closed state. The liquid phase outlets of the nonene reactor A, the nonene reactor B, and the nonene reactor C are all equipped with full-component online analyzers to detect the product flow rate and propylene concentration, and calculate the propylene conversion rate. When the propylene conversion rate detected at the outlet of the nonene reactor A is less than the set value of 50%-60%, the nonene reactor A needs to be stopped and the reactor C needs to be switched into operation. The specific operation steps are as follows: the automatic control unit starts the control module after processing according to the collected data to make the system enter the reactor switching program, realize one-key automatic switching, open the heat exchange valve of the nonene reactor C, preheat the nonene reactor C through the heat exchanger, and the water in the drum gradually heats up. The hot water heats the nonene reactor C through the shell side. The flow rate of the high-pressure steam of the heat exchanger is controlled by the temperature indicating controller TIC at the outlet of the heat exchanger. When the temperature is higher than 135-145°C, the opening of the heat exchange valve is adjusted to 5-15%; when the temperature is lower than 85-95°C, the opening of the heat exchange valve is adjusted to 85-95%. At this time, the water in the nonene reactor C flows counterclockwise. Since the reaction in the nonene reactor C is an exothermic reaction, when the water temperature rises to about 80-150°C, the heat exchange valve is closed, and the heat released by the nonene reactor C reaction itself is used to raise the temperature of the reaction to the normal operating temperature. The reaction temperature is detected by the temperature detector TT on the nonene reactor C. At this time, the heat released by the polymerization reaction is withdrawn through the water on the shell side, and the low-temperature water in the drum enters the shell side of the nonene reactor C by gravity, absorbs the reaction heat and partially vaporizes into a two-phase flow and enters the drum. After gas-liquid separation in the drum, the top can produce steam of a certain pressure for recycling. In normal operation, the water on the shell side of the nonene reactor C flows clockwise; after the data acquisition module collects the temperature on the shell side of the nonene reactor C and preheats it to 80-150°C, the valve openings on the feed pipe and discharge pipe of the nonene reactor C are gradually increased until they are fully opened, and the nonene reactor C Normal operation; at the same time, gradually reduce the valve opening on the feed pipeline of nonene reactor A to fully closed. At this time, the valves on the feed pipeline and the discharge pipeline of nonene reactor A are fully closed, nonene reactor A is cut out from the system, and the valves on the oil and gas recovery pipeline and the liquid recovery pipeline of nonene reactor A are opened. The gas phase is sent from the top to the oil and gas recovery system, and the liquid phase is sent from the bottom to the recovery tank. At this time, the system will switch to normal operation of nonene reactor B and nonene reactor C, and nonene reactor A is on standby. The rate of gradually increasing and decreasing the valve is the same, which is 25-50% / h.

[0066] The present invention uses the propylene conversion rate at the outlet of the nonene reactor as a monitoring indicator. When the outlet conversion rate of the nonene reactor in operation is less than a set value, the switching of the parallel reactors of the reaction system and the switching of the internal heating heat exchanger can be quickly achieved through the delayed interlocking one-key switching program of automatic control, thereby increasing safety and reliability, improving work efficiency, reducing operating workload, and achieving better technical effects. BRIEF DESCRIPTION OF THE DRAWINGS

[0067] Figure 1 is a schematic structural diagram of a nonene production system of Example 1-3;

[0068] Figure 2 It is a schematic diagram of the structure of the preheating device of Example 1-3;

[0069] Figure 3 It is a schematic diagram of the structure of the lower head filter screen of Example 1-2;

[0070] Figure 4 This is a schematic diagram of the structure of the lower head filter screen of Example 3.

[0071] Among them, A-nonene reactor A, B-nonene reactor B, C-nonene reactor C, D-steam drum, E-heat exchanger, 1-valve 1, 2-valve 2, 3-valve 3, 4-valve 4, 5-valve 5, 6-valve 6, 7-valve 7, 8-valve 8, 9-valve 9, 10-valve 10, 11-valve 11, 12-valve 12, 13-heat exchange valve 13, 14-heat exchange valve 14, 15-lower head filter, 16-drainage pipe, 17-material outlet, 18-discharge port, 19-conical structure, 20-columnar structure (filter structure). DETAILED DESCRIPTION

[0072] The present invention is described in detail below in conjunction with specific drawings and embodiments. It is necessary to point out that the following embodiments are only used to further illustrate the present invention and cannot be understood as limiting the scope of protection of the present invention. Some non-essential improvements and adjustments made to the present invention by those skilled in the art based on the content of the present invention still fall within the scope of protection of the present invention.

[0073] The specific equipment involved below are all existing products and will not be described in detail here.

[0074] Example 1

[0075] like Figure 1As shown, the nonene production system includes three nonene reactors connected in parallel: nonene reactor A, nonene reactor B and nonene reactor C. A full-component online analyzer is provided at the bottom liquid phase outlet of each nonene reactor. Feed pipelines are provided on nonene reactor A, nonene reactor B and nonene reactor C, respectively. Valve 1 is installed on the feed pipeline of nonene reactor A, valve 3 is installed on the feed pipeline of nonene reactor B, and valve 5 is installed on the feed pipeline of nonene reactor C. Oil and gas recovery pipelines are provided on the tops of nonene reactor A, nonene reactor B and nonene reactor C, respectively. Valve 7. A valve 9 is installed on the oil and gas recovery pipeline of the nonene reactor B, a valve 11 is installed on the oil and gas recovery pipeline of the nonene reactor C, the liquid phase outlets at the bottom of the nonene reactor A, the nonene reactor B and the nonene reactor C are respectively connected to the discharge pipeline and the liquid phase recovery pipeline, the discharge pipeline of the nonene reactor A is installed with a valve 2, the discharge pipeline of the nonene reactor B is installed with a valve 4, the discharge pipeline of the nonene reactor C is installed with a valve 6, the liquid phase recovery pipeline of the nonene reactor A is installed with a valve 8, the liquid phase recovery pipeline of the nonene reactor B is installed with a valve 10, and the liquid phase recovery pipeline of the nonene reactor C is installed with a valve 12.

[0076] like Figure 2 As shown, the nonene reactor A, the nonene reactor B and the nonene reactor C are respectively equipped with preheating devices, which include: a steam drum D connected with the shell side of the nonene reactor through a preheating pipe and a heat exchanger E connected in parallel to the preheating pipe, a heat exchange valve 13 and a heat exchange valve 14 are respectively installed on both sides of the heat exchanger E, a temperature indicating controller is provided at the water outlet of the heat exchanger E, and the temperature indicating controller is electrically connected to the heat exchange valve 13 and the heat exchange valve 14 respectively, a steam recovery pipeline is provided on the steam drum D, and temperature detectors are respectively provided on the shell side of the nonene reactor A, the nonene reactor B and the nonene reactor C.

[0077] The nonene production system of the present invention is provided with an automated control unit, including a data acquisition module, a data processing module and a control module which are connected in sequence; the data acquisition module is electrically connected to the full-component online analyzers of the nonene reactor A, the nonene reactor B and the nonene reactor C, respectively, and the data acquisition module is electrically connected to the temperature detectors on the shell side of the nonene reactor A, the nonene reactor B and the nonene reactor C, respectively; the control module is electrically connected to the valves 1 to 12, respectively, and the control module is electrically connected to the heat exchange valve 13 and the heat exchange valve 14, respectively.

[0078] like Figure 3As shown, a lower head filter 15 is installed in the lower head of the nonene reactor A, the nonene reactor B and the nonene reactor C respectively, a material outlet 17 is arranged at the bottom of the lower head of the nonene reactor, a drainage pipe 16 of the lower head filter 15 is arranged above the material outlet 17 at the bottom of the nonene reactor and is connected thereto, a discharge port 18 is arranged beside the material outlet 17, and the nominal diameter of the discharge port 18 is 150 mm (DN150); the upper part of the lower head filter 15 is a conical structure 19 which is narrow at the top and wide at the bottom, the conical structure 19 is a cone, and the side wall of the conical structure 19 is a closed smooth inclined surface with a slope angle of 40°, and the lower part of the lower head filter 15 is a columnar structure 2 0, the bottom edge of the conical structure 19 is consistent with the top edge of the columnar structure 20 and is connected. The columnar structure 20 is a cylinder. The side wall and the bottom of the columnar structure 20 are both filter structures. The filter structure is a wire mesh with a mesh size of 100. A through hole is provided at the bottom of the columnar structure 20. A drainage pipe 16 is connected downwardly through the through hole. The nominal diameter of the drainage pipe 16 matches the material outlet 17 of the nonene reactor. The height of the drainage pipe 16 is 500 mm. The bottom diameter of the conical structure 19 is 800 mm (DN800). The lower head filter 15 is made of 321 stainless steel. The total height of the lower head filter 15 is 1300 mm. The height of the columnar structure 20 is 300 mm.

[0079] When the nonene reactor A and the nonene reactor B are in normal operation, the nonene reactor A and the nonene reactor B are operating reactors, and the nonene reactor C is a standby reactor. At this time, valves 1, 2, 3, and 4 on the feed and discharge pipes of the nonene reactor A and the nonene reactor B are in an open state, and valves 5 and 6 on the feed and discharge pipes of the nonene reactor C are in a closed state. The liquid phase outlets of the nonene reactor A, the nonene reactor B, and the nonene reactor C are all equipped with full-component online analyzers to detect the product flow rate and propylene concentration, and calculate the propylene conversion rate. The online analyzer sends the propylene conversion rate to the data acquisition module, and the data acquisition module sends the data to the data processing module. The data processing module compares the data. If the propylene conversion rate is less than 50%, the data processing module notifies the control module control system to perform the reactor switching program to achieve one-key automatic switching. At this time, it is necessary to stop the nonene reactor A and put the reactor C into operation, which specifically includes: opening the heat exchange valve 13 and the heat exchange valve 14, preheating the nonene reactor C through the heat exchanger E, gradually heating the water in the drum D, and heating the hot water through the shell side of the nonene reactor C. The flow rate of the high-pressure steam of the heat exchanger is controlled by the temperature indicating controller TIC at the outlet of the heat exchanger E. When the temperature is higher than 135°C, the opening of the heat exchange valve is adjusted to 5%; when the temperature is lower than 85°C, the opening of the heat exchange valve is adjusted to 85%. At this time, the water in the nonene reactor C flows counterclockwise. Since the reaction in the nonene reactor C is an exothermic reaction, when the water temperature sent by the temperature detector TT rises to the set temperature of 80°C, the control module closes the heat exchange valve 13 and the heat exchange valve 14, and uses the heat released by the reaction of the nonene reactor C to raise the temperature to the normal operating temperature. At this time, the heat released by the polymerization reaction is withdrawn through the water in the shell side, and the low-temperature water in the drum D enters the shell side of the nonene reactor C by gravity, absorbs the heat of reaction and partially vaporizes into a two-phase flow to enter the drum. After gas-liquid separation in the drum D, the steam with a certain pressure produced as a byproduct on the top can be recycled. In normal operation, the water in the shell side of the nonene reactor C flows clockwise. When the water temperature sent by the temperature detector TT rises to the set temperature of 80°C, the control module gradually increases the opening of valves 5 and 6 on the feed pipe and discharge pipe of nonene reactor C until they are fully opened, and nonene reactor C operates normally. At the same time, the opening of valve 1 on the feed pipe of nonene reactor A is gradually reduced to fully closed. At this time, valves 1 and 2 on the feed pipe and discharge pipe of nonene reactor A are fully closed, nonene reactor A is cut out of the system, and valves 7 and 8 on the oil and gas recovery pipe and liquid recovery pipe of nonene reactor A are opened. The gas phase is sent from the top to the oil and gas recovery system, and the liquid phase is sent from the bottom to the recovery tank. The rate of gradually increasing and decreasing valves 5, 6 and 1 is the same, which is 25% / h. Valves 1 to 12 and heat exchange valves 13 and 14 are delayed interlock valves with a delay time of 1 min.At this time, the system switches to a state where the nonene reactor B and the nonene reactor C operate normally, and the nonene reactor A is on standby.

[0080] Example 2

[0081] Continue as Figure 1 As shown, the nonene production system includes three nonene reactors connected in parallel: nonene reactor A, nonene reactor B and nonene reactor C. A full-component online analyzer is provided at the bottom liquid phase outlet of each nonene reactor. Feed pipelines are provided on nonene reactor A, nonene reactor B and nonene reactor C, respectively. Valve 1 is installed on the feed pipeline of nonene reactor A, valve 3 is installed on the feed pipeline of nonene reactor B, and valve 5 is installed on the feed pipeline of nonene reactor C. Oil and gas recovery pipelines are provided on the tops of nonene reactor A, nonene reactor B and nonene reactor C, respectively. Valve 7. A valve 9 is installed on the oil and gas recovery pipeline of the nonene reactor B, a valve 11 is installed on the oil and gas recovery pipeline of the nonene reactor C, the liquid phase outlets at the bottom of the nonene reactor A, the nonene reactor B and the nonene reactor C are respectively connected to the discharge pipeline and the liquid phase recovery pipeline, the discharge pipeline of the nonene reactor A is installed with a valve 2, the discharge pipeline of the nonene reactor B is installed with a valve 4, the discharge pipeline of the nonene reactor C is installed with a valve 6, the liquid phase recovery pipeline of the nonene reactor A is installed with a valve 8, the liquid phase recovery pipeline of the nonene reactor B is installed with a valve 10, and the liquid phase recovery pipeline of the nonene reactor C is installed with a valve 12.

[0082] Continue as Figure 2 As shown, the nonene reactor A, the nonene reactor B and the nonene reactor C are respectively equipped with preheating devices, which include: a steam drum D connected with the shell side of the nonene reactor through a preheating pipe and a heat exchanger E connected in parallel to the preheating pipe, a heat exchange valve 13 and a heat exchange valve 14 are respectively installed on both sides of the heat exchanger E, a temperature indicating controller is provided at the water outlet of the heat exchanger E, and the temperature indicating controller is electrically connected to the heat exchange valve 13 and the heat exchange valve 14 respectively, a steam recovery pipeline is provided on the steam drum D, and temperature detectors are respectively provided on the shell side of the nonene reactor A, the nonene reactor B and the nonene reactor C.

[0083] The nonene production system of the present invention is provided with an automated control unit, including a data acquisition module, a data processing module and a control module which are connected in sequence; the data acquisition module is electrically connected to the full-component online analyzers of the nonene reactor A, the nonene reactor B and the nonene reactor C, respectively, and the data acquisition module is electrically connected to the temperature detectors on the shell side of the nonene reactor A, the nonene reactor B and the nonene reactor C, respectively; the control module is electrically connected to the valves 1 to 12, respectively, and the control module is electrically connected to the heat exchange valve 13 and the heat exchange valve 14, respectively.

[0084] Continue as Figure 3 As shown, a lower head filter 15 is installed in the lower head of the nonene reactor A, the nonene reactor B and the nonene reactor C respectively, a material outlet 17 is arranged at the bottom of the lower head of the nonene reactor, a drainage pipe 16 of the lower head filter 15 is arranged above the material outlet 17 at the bottom of the nonene reactor and is connected thereto, a discharge port 18 is arranged beside the material outlet 17, and the nominal diameter of the discharge port 18 is 200 mm (DN200); the upper part of the lower head filter 15 is a conical structure 19 which is narrow at the top and wide at the bottom, the conical structure 19 is a cone, and the side wall of the conical structure 19 is a closed smooth inclined surface, and the slope angle of the smooth inclined surface is 45°, and the lower part of the lower head filter 15 is a columnar structure 20 The bottom edge of the conical structure 19 is consistent in shape with the top edge of the columnar structure 20 and is connected. The columnar structure 20 is a cylinder. The side wall and the bottom of the columnar structure 20 are both filter structures. The filter structure is a wire mesh with a mesh size of 150. A through hole is provided at the bottom of the columnar structure 20. The through hole is downwardly connected to a drainage pipe 16. The nominal diameter of the drainage pipe 16 matches the material outlet 17 of the nonene reactor. The height of the drainage pipe 16 is 600 mm. The bottom diameter of the conical structure 19 is 1000 mm (DN1000). The lower head filter 15 is made of 321 stainless steel. The total height of the lower head filter 15 is 1500 mm. The height of the columnar structure 20 is 200 mm.

[0085] When the nonene reactor A and the nonene reactor B are in normal operation, the nonene reactor A and the nonene reactor B are operating reactors, and the nonene reactor C is a standby reactor. At this time, valves 1, 2, 3, and 4 on the feed and discharge pipes of the nonene reactor A and the nonene reactor B are in an open state, and valves 5 and 6 on the feed and discharge pipes of the nonene reactor C are in a closed state. The liquid phase outlets of the nonene reactor A, the nonene reactor B, and the nonene reactor C are all equipped with full-component online analyzers to detect the product flow rate and propylene concentration, and calculate the propylene conversion rate. The online analyzer sends the propylene conversion rate to the data acquisition module, and the data acquisition module sends the data to the data processing module. The data processing module compares the data. If the propylene conversion rate is less than 55%, the data processing module notifies the control module control system to perform the reactor switching program to achieve one-key automatic switching. At this time, it is necessary to stop the nonene reactor A and put the reactor C into operation, which specifically includes: opening the heat exchange valve 13 and the heat exchange valve 14, preheating the nonene reactor C through the heat exchanger E, gradually heating the water in the drum D, and heating the hot water through the shell side of the nonene reactor C. The flow rate of the high-pressure steam of the heat exchanger is controlled by the temperature indicating controller TIC at the outlet of the heat exchanger E. When the temperature is higher than 140°C, the opening of the heat exchange valve is adjusted to 10%; when the temperature is lower than 90°C, the opening of the heat exchange valve is adjusted to 90%. At this time, the water in the nonene reactor C flows counterclockwise. Since the reaction in the nonene reactor C is an exothermic reaction, when the water temperature sent by the temperature detector TT rises to the set temperature of 120°C, the control module closes the heat exchange valve 13 and the heat exchange valve 14, and uses the heat released by the reaction of the nonene reactor C to raise the temperature to the normal operating temperature. At this time, the heat released by the polymerization reaction is withdrawn through the water in the shell side, and the low-temperature water in the drum D enters the shell side of the nonene reactor C by gravity, absorbs the reaction heat and partially vaporizes into a two-phase flow to enter the drum. After gas-liquid separation in the drum D, the steam with a certain pressure produced as a byproduct on the top can be recycled. In normal operation, the water in the shell side of the nonene reactor C flows clockwise. When the water temperature sent by the temperature detector TT rises to the set temperature of 120°C, the control module gradually increases the opening of valves 5 and 6 on the feed pipe and discharge pipe of nonene reactor C until they are fully opened, and nonene reactor C operates normally. At the same time, the opening of valve 1 on the feed pipe of nonene reactor A is gradually reduced to fully closed. At this time, valves 1 and 2 on the feed pipe and discharge pipe of nonene reactor A are fully closed, nonene reactor A is cut out of the system, and valves 7 and 8 on the oil and gas recovery pipe and liquid recovery pipe of nonene reactor A are opened. The gas phase is sent from the top to the oil and gas recovery system, and the liquid phase is sent from the bottom to the recovery tank. The rate of gradually increasing and decreasing valves 5, 6 and 1 is the same, which is 35% / h. Valves 1 to 12 and heat exchange valves 13 and 14 are delayed interlock valves with a delay time of 3 minutes.At this time, the system switches to a state where the nonene reactor B and the nonene reactor C operate normally, and the nonene reactor A is on standby.

[0086] Example 3

[0087] Continue as Figure 1 As shown, the nonene production system includes three nonene reactors connected in parallel: nonene reactor A, nonene reactor B and nonene reactor C. A full-component online analyzer is provided at the bottom liquid phase outlet of each nonene reactor. Feed pipelines are provided on nonene reactor A, nonene reactor B and nonene reactor C, respectively. Valve 1 is installed on the feed pipeline of nonene reactor A, valve 3 is installed on the feed pipeline of nonene reactor B, and valve 5 is installed on the feed pipeline of nonene reactor C. Oil and gas recovery pipelines are provided on the tops of nonene reactor A, nonene reactor B and nonene reactor C, respectively. Valve 7. A valve 9 is installed on the oil and gas recovery pipeline of the nonene reactor B, a valve 11 is installed on the oil and gas recovery pipeline of the nonene reactor C, the liquid phase outlets at the bottom of the nonene reactor A, the nonene reactor B and the nonene reactor C are respectively connected to the discharge pipeline and the liquid phase recovery pipeline, the discharge pipeline of the nonene reactor A is installed with a valve 2, the discharge pipeline of the nonene reactor B is installed with a valve 4, the discharge pipeline of the nonene reactor C is installed with a valve 6, the liquid phase recovery pipeline of the nonene reactor A is installed with a valve 8, the liquid phase recovery pipeline of the nonene reactor B is installed with a valve 10, and the liquid phase recovery pipeline of the nonene reactor C is installed with a valve 12.

[0088] Continue as Figure 2 As shown, the nonene reactor A, the nonene reactor B and the nonene reactor C are respectively equipped with preheating devices, which include: a steam drum D connected with the shell side of the nonene reactor through a preheating pipe and a heat exchanger E connected in parallel to the preheating pipe, a heat exchange valve 13 and a heat exchange valve 14 are respectively installed on both sides of the heat exchanger E, a temperature indicating controller is provided at the water outlet of the heat exchanger E, and the temperature indicating controller is electrically connected to the heat exchange valve 13 and the heat exchange valve 14 respectively, a steam recovery pipeline is provided on the steam drum D, and temperature detectors are respectively provided on the shell side of the nonene reactor A, the nonene reactor B and the nonene reactor C.

[0089] The nonene production system of the present invention is provided with an automated control unit, including a data acquisition module, a data processing module and a control module which are connected in sequence; the data acquisition module is electrically connected to the full-component online analyzers of the nonene reactor A, the nonene reactor B and the nonene reactor C, respectively, and the data acquisition module is electrically connected to the temperature detectors on the shell side of the nonene reactor A, the nonene reactor B and the nonene reactor C, respectively; the control module is electrically connected to the valves 1 to 12, respectively, and the control module is electrically connected to the heat exchange valve 13 and the heat exchange valve 14, respectively.

[0090] like Figure 4 As shown, a lower head filter 15 is installed in the lower head of the nonene reactor A, the nonene reactor B and the nonene reactor C respectively, a material outlet 17 is arranged at the bottom of the lower head of the nonene reactor, a drainage pipe 16 of the lower head filter 15 is arranged above the material outlet 17 at the bottom of the nonene reactor and is connected thereto, a discharge port 18 is arranged beside the material outlet 17, and the nominal diameter of the discharge port 18 is 250 mm (DN250); the upper part of the lower head filter 15 is a conical structure 19 which is narrow at the top and wide at the bottom, the conical structure 19 is a truncated cone, the side wall of the conical structure 19 is a closed smooth inclined surface, the slope angle of the smooth inclined surface is 55°, and the lower part of the lower head filter 15 is a columnar structure 20 The bottom edge of the conical structure 19 is consistent in shape with the top edge of the columnar structure 20 and is connected. The columnar structure 20 is a cylinder. The side wall and the bottom of the columnar structure 20 are filter structures. The filter structure is a wire mesh with a mesh size of 200. A through hole is provided at the bottom of the columnar structure 20. A drainage pipe 16 is connected downwardly through the through hole. The nominal diameter of the drainage pipe 16 matches the material outlet 17 of the nonene reactor. The height of the drainage pipe 16 is 800 mm. The bottom diameter of the conical structure 19 is 1200 mm (DN1200). The lower head filter 15 is made of 321 stainless steel. The total height of the lower head filter 15 is 1700 mm. The height of the columnar structure 20 is 400 mm.

[0091] When the nonene reactor A and the nonene reactor B are in normal operation, the nonene reactor A and the nonene reactor B are operating reactors, and the nonene reactor C is a standby reactor. At this time, valves 1, 2, 3, and 4 on the feed and discharge pipes of the nonene reactor A and the nonene reactor B are in an open state, and valves 5 and 6 on the feed and discharge pipes of the nonene reactor C are in a closed state. The liquid phase outlets of the nonene reactor A, the nonene reactor B, and the nonene reactor C are all equipped with full-component online analyzers to detect the product flow rate and propylene concentration, and calculate the propylene conversion rate. The online analyzer sends the propylene conversion rate to the data acquisition module, and the data acquisition module sends the data to the data processing module. The data processing module compares the data. If the propylene conversion rate is less than 60%, the data processing module notifies the control module control system to perform the reactor switching program to achieve one-key automatic switching. At this time, it is necessary to stop the nonene reactor A and put the reactor C into operation, which specifically includes: opening the heat exchange valve 13 and the heat exchange valve 14, preheating the nonene reactor C through the heat exchanger E, gradually heating the water in the drum D, and heating the hot water through the shell side of the nonene reactor C. The flow rate of the high-pressure steam of the heat exchanger is controlled by the temperature indicating controller TIC at the outlet of the heat exchanger E. When the temperature is higher than 145°C, the opening of the heat exchange valve is adjusted to 15%; when the temperature is lower than 95°C, the opening of the heat exchange valve is adjusted to 95%. At this time, the water in the nonene reactor C flows counterclockwise. Since the reaction in the nonene reactor C is an exothermic reaction, when the water temperature sent by the temperature detector TT rises to the set temperature of 150°C, the control module closes the heat exchange valve 13 and the heat exchange valve 14, and uses the heat released by the reaction of the nonene reactor C to raise the temperature to the normal operating temperature. At this time, the heat released by the polymerization reaction is withdrawn through the water in the shell side, and the low-temperature water in the drum D enters the shell side of the nonene reactor C by gravity, absorbs the reaction heat and partially vaporizes into a two-phase flow to enter the drum. After gas-liquid separation in the drum D, the steam with a certain pressure produced as a by-product at the top can be recycled. In normal operation, the water in the shell side of the nonene reactor C flows clockwise. When the water temperature sent by the temperature detector TT rises to the set temperature of 150°C, the control module gradually increases the opening of valves 5 and 6 on the feed pipe and discharge pipe of nonene reactor C until they are fully opened, and nonene reactor C operates normally. At the same time, the opening of valve 1 on the feed pipe of nonene reactor A is gradually reduced to fully closed. At this time, valves 1 and 2 on the feed pipe and discharge pipe of nonene reactor A are fully closed, nonene reactor A is cut out of the system, and valves 7 and 8 on the oil and gas recovery pipe and liquid recovery pipe of nonene reactor A are opened. The gas phase is sent from the top to the oil and gas recovery system, and the liquid phase is sent from the bottom to the recovery tank. The rate of gradually increasing and decreasing valves 5, 6 and 1 is the same, which is 50% / h. Valves 1 to 12 and heat exchange valves 13 and 14 are delayed interlock valves with a delay time of 5 minutes.At this time, the system switches to a state where the nonene reactor B and the nonene reactor C operate normally, and the nonene reactor A is on standby.

[0092] A nonene production system and automatic switching method thereof provided in Examples 1-3 can realize one-button automatic switching, complete the functions of stopping the reactor, recovering residual materials, and starting the heater switching, without manual operation, thereby greatly reducing the risks brought about thereby; and the nonene reactor of the present invention adds a lower head filter in the lower head of the nonene reactor. When the nonene reactor is switched every 3 months, the lower head filter is cleaned, and the operator no longer needs to frequently clean valve A, thereby ensuring that the heat transfer effect and pressure drop of the downstream heat exchanger meet the process requirements.

Claims

1. A nonene production system, Features The system comprises: At least three nonene reactors connected in parallel, at least one of which is used as a standby reactor and the rest are operating reactors; Each of the nonene reactors is provided with a feed port at the top and a liquid phase discharge port at the bottom; a full-component online analyzer is provided at the bottom liquid phase discharge port; the feed port at the top of each nonene reactor is respectively connected to the feed pipeline and the oil and gas recovery pipeline, and the liquid phase discharge port at the bottom of each nonene reactor is respectively connected to the discharge pipeline and the liquid phase recovery pipeline; valves are respectively installed on the feed pipeline, oil and gas recovery pipeline, discharge pipeline and liquid phase recovery pipeline of each nonene reactor, and each nonene reactor is equipped with a preheating device.

2. The nonene production system according to claim 1, Features: The preheating device comprises: a steam drum and a heat exchanger; The steam drum is connected with the shell side of the nonene reactor through a preheating pipe, and the heat exchanger is connected in parallel to the preheating pipe.

3. The nonene production system according to claim 2, Features: Heat exchange valves are installed on both sides of the heat exchanger, and a temperature indicating controller is arranged at the outlet end of the heat exchanger, and the temperature indicating controller is electrically connected to the heat exchange valve.

4. The nonene production system according to claim 2, Features: The steam drum is provided with a steam recovery pipeline; and / or, A temperature detector is provided on the shell side of each nonene reactor.

5. The nonene production system according to any one of claims 1 to 4, Features: The system is provided with an automatic control unit, which comprises a data acquisition module, a data processing module and a control module which are connected in sequence.

6. The nonene production system according to claim 5, Features: The data acquisition module is electrically connected to the full-component online analyzer of each nonene reactor; the data acquisition module is electrically connected to the temperature detector on the shell side of each nonene reactor; The control module is electrically connected to the valves on the feed pipeline, oil and gas recovery pipeline, discharge pipeline and liquid phase recovery pipeline of each nonene reactor respectively; the control module is electrically connected to the heat exchange valve of each nonene reactor respectively.

7. The nonene production system according to claim 1, Features: A lower head filter is arranged in the lower head of each nonene reactor, the upper part of the lower head filter is a conical structure which is narrow at the top and wide at the bottom, the side wall of the conical structure is a closed smooth inclined surface, the lower part of the lower head filter is a columnar structure, the side wall and the bottom of the columnar structure are both filter structures, a through hole is arranged at the bottom of the columnar structure, a drainage pipe is connected downwardly to the through hole, a material outlet is arranged at the bottom of the lower head in the nonene reactor, and the drainage pipe of the lower head filter is arranged above the material outlet at the bottom of the nonene reactor and is connected thereto.

8. The nonene production system according to claim 7, Features: The bottom edge of the conical structure is consistent in shape with the top edge of the columnar structure and is connected; and / or, The conical structure is a cone or a frustum; preferably, a cone, a pyramid, a truncated cone or a prism; and / or, The columnar structure is a cylinder or a prism; and / or, The slope angle of the smooth slope is greater than or equal to the sliding angle of the catalyst, preferably 40° to 55°; and / or, The filter structure is a wire mesh, and / or the mesh number of the filter structure is 100 to 800 meshes, preferably 200 to 800 meshes; and / or, The nominal diameter of the draft tube matches the material outlet of the nonene reactor; and / or, The height of the drainage tube is 500 mm to 800 mm.

9. The nonene production system according to claim 8, Features: The bottom diameter of the cone-shaped structure is 800-1200 mm; preferably, when the cone-shaped structure is a pyramid or a prism, the bottom area of ​​the cone-shaped structure is 0.5 m 2 ~1.2m 2 and / or, The lower head filter screen is made of 321 stainless steel or titanium alloy; and / or, The total height of the lower head filter is 1300mm-1700mm; and / or, The height of the columnar structure is 200 to 400 mm; and / or, A discharge port is provided at the bottom of the nonene reactor; preferably, the discharge port is arranged beside the material outlet; more preferably, the nominal diameter of the discharge port is 150-250 mm.

10. An automatic switching method for a nonene production system according to any one of claims 1 to 9, Features The method comprises: The automatic control unit compares the propylene conversion rate sent by the full-component online analyzer with the set value. If the propylene conversion rate is less than the set value, the control system enters the reactor switching program; The reactor switching procedure includes: After the preheating device of the standby reactor is turned on for preheating, the valves on the feed pipe and the discharge pipe of the standby reactor are opened, and the standby reactor is switched to the operating reactor; At the same time, the valves on the feed pipe and discharge pipe of the operating reactor whose propylene conversion rate is less than the set value are closed, and the valve on the liquid phase recovery pipe of its oil and gas recovery pipe is opened. At this time, the operating reactor is switched to the standby reactor.

11. The automatic switching method according to claim 10, Features: After the preheating device of the standby reactor is opened for preheating, the operation of opening the valves on the feed pipe and the discharge pipe of the standby reactor comprises: The preheating device of the standby reactor is turned on for preheating, and the automatic control unit compares the temperature sent by the temperature detector with the set temperature. When the temperature is the same as the set temperature, the automatic control unit gradually increases the opening of the valves on the feed pipe and the discharge pipe of the standby reactor until they are fully opened; The operation of closing the valves on the feed pipe and the discharge pipe of the operating reactor whose propylene conversion rate is less than the set value includes: The automatic control unit gradually reduces the opening of the valves on the feed pipe and the discharge pipe of the operating reactor whose propylene conversion rate is less than the set value to fully close, and opens the valve on the liquid phase recovery pipe of its oil and gas recovery pipe.

12. The automatic switching method according to claim 10 or 11, Features: The set value of the propylene conversion rate is 50%-60%, preferably 55%-60%; and / or, The preheating setting temperature is 80-150° C.; and / or, The rate of gradually increasing and decreasing the valve is the same, preferably 25-50% / h; and / or, The valves on the feed pipeline, oil and gas recovery pipeline, discharge pipeline and liquid phase recovery pipeline of each nonene reactor and the heat exchange valve of each nonene reactor are delayed interlock valves, and preferably, the delay time is 1 to 5 minutes.

13. The automatic switching method according to claim 10 or 11, Features The starting of the preheating device includes: The control module of the automatic control unit opens the heat exchange valve of the preheating device, and the heat exchanger heats the heat exchange medium. After the heat exchange medium in the drum is heated, it enters the shell side of the nonene reactor to preheat the reactor; preferably, the heat exchange medium is water.

14. The automatic switching method according to claim 13, Features: During the preheating process of the preheating device, the steam flow rate of the heat exchanger is controlled by the controller according to the temperature indicating the outlet of the heat exchanger; Preferably, When the temperature is higher than 135-145°C, adjust the opening of the heat exchange valve to 5-15%; when the temperature is lower than 85-95°C, adjust the opening of the heat exchange valve to 85-95%.

15. The automatic switching method according to claim 13, Features: The automatic control unit compares the shell temperature of the nonene reactor sent by the temperature detector with the set temperature. When the temperature is the same as the set temperature, the automatic control unit closes the heat exchange valves on both sides of the heat exchanger. Preferably, the set temperature is 80-150°C.

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