CN221182712U - Automatic circulation material returning device for high-temperature pressurized fluidized bed reactor without dilute phase zone - Google Patents
Automatic circulation material returning device for high-temperature pressurized fluidized bed reactor without dilute phase zone Download PDFInfo
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- CN221182712U CN221182712U CN202323082526.2U CN202323082526U CN221182712U CN 221182712 U CN221182712 U CN 221182712U CN 202323082526 U CN202323082526 U CN 202323082526U CN 221182712 U CN221182712 U CN 221182712U
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The utility model discloses automatic circulating and returning equipment for a high-temperature pressurized fluidized bed reactor without a dilute phase zone, which comprises the high-temperature pressurized fluidized bed reactor without the dilute phase zone, a reactor outlet pipe, a circulating and returning component and a returning component; the high-temperature pressurized fluidized bed reactor without the dilute phase zone is not provided with the dilute phase zone, one end of a reactor outlet pipe is communicated with a gas outlet of the high-temperature pressurized fluidized bed reactor without the dilute phase zone, a circulating material returning assembly is externally arranged in the high-temperature pressurized fluidized bed reactor without the dilute phase zone, and the other end of the reactor outlet pipe is communicated with an inlet end of the circulating material returning assembly; the outlet end of the circulating return assembly is connected with the feed inlet of the return assembly, and the discharge outlet of the return assembly is communicated with the high-temperature pressurized fluidized bed reactor without dilute phase region. The utility model relates to the technical field of chemical gas-solid two-phase reaction equipment, and can solve the problems of large reactor volume and high cost caused by the fact that a multi-stage cyclone separator is arranged in a fluidized bed reactor in the prior art.
Description
Technical Field
The utility model relates to the technical field of chemical gas-solid two-phase reaction equipment, in particular to automatic circulation material returning equipment for a high-temperature pressurized fluidized bed reactor without a dilute phase zone.
Background
The fluidized bed is a bed form in which fluid is utilized to pass through a granular solid bed, and when the resistance of the fluid flowing through the bed is greater than the weight of the bed particles, the solid particles are in a suspension motion state and can flow like the fluid. The corresponding reactor is a fluidized bed reactor, and particles in the fluidized bed reactor can flow freely as fluid, so that the fluidized bed reactor has the following main advantages: the bed layer has high-efficiency heat transfer performance, the temperature inside the bed layer is uniform and easy to control, and the method is particularly suitable for a strong exothermic reaction system; the continuous reaction and the regeneration circulation operation of solid powder materials or catalyst particles can be realized, and the catalyst is suitable for reactions with faster catalyst deactivation; the continuous input and output of the solid materials can be realized through a separation system. Based on the advantages, the fluidized bed reactor is rapidly developed in the fields of chemical engineering, petrochemical industry and coal chemical industry.
The gas-solid two-phase fluidized bed reactor has a plurality of structural types, but is generally composed of a gas distribution device, an internal member, a heat exchange device, a gas-solid separation device and the like no matter what the types are. The fluidized bed is divided into a dense phase zone (dense phase section), a transition zone and a dilute phase zone (separation section) along the height direction. The region below the bed interface of the fluidized bed is called dense phase region, and the region above the bed interface is called dilute phase region. Because some fluidized beds have higher fluidization gas velocity and larger diameter, bed interfaces are not obvious, so that the area between the dense-phase area and the dilute-phase area is often called a transition area, and the total height of the fluidized bed is the sum of the heights of the dense-phase area, the transition area and the dilute-phase area. The solid particles (powder materials or catalysts) in the fluidized bed have certain particle size distribution, and meanwhile, during the operation of the fluidized bed, some fine particles are generated due to collision and abrasion among the particles, so that the sedimentation speed of a part of fine particles in the particles of the fluidized bed is lower than the airflow speed, and the particles are carried out of the reactor by gas after passing through a dilute phase zone when being carried out of a dense phase zone. In addition, as the gas passes through the fluidised bed, the bubbles break up at the bed surface and throw some of the solid particles into the dilute phase zone, most of these particles settling at a rate greater than the gas flow rate, and so they fall back to the bed after reaching a certain height. Thus, the concentration of the solid particles in the region which is far away from the bed surface is smaller, and the concentration of the solid particles is basically unchanged after a certain distance from the bed surface. The minimum distance that the concentration of solid particles begins to remain unchanged is called the separation zone height (also called the TDH height). A freeboard zone must be present above the bed interface (or transition zone) of a conventional fluidized bed to allow particles having a settling velocity greater than the velocity of the gas stream to redeposit into the dense phase zone without being carried away by the gas stream. In order to reduce the TDH height of the fluidized bed, the upper part of many fluidized beds is also provided with an expansion section, i.e. the diameter of the dilute phase zone of the fluidized bed is larger than that of the dense phase zone.
Because the solids (or catalyst) concentration in the dilute phase zone of a conventional fluidized bed is still relatively high, if the solids (or catalyst) are not recovered by a gas-solid separation device, a large amount of solid particles can escape from the outlet of the fluidized bed reactor, and not only can a large amount of useful unreacted solids be lost, but also the finally produced products can be polluted, so that the gas-solid separation device is generally arranged in the dilute phase zone of the conventional fluidized bed reactor for capturing the solid particles (or catalyst). For example, the high-efficiency cyclone separator and the high-temperature filter are the most common and practical, and the high-efficiency cyclone separator arranged in the dilute phase zone can also adopt a multi-stage multi-group mode to improve the solid particle separation efficiency in consideration of the use limitation of the high-temperature filter. In order to meet the requirements of a built-in cyclone separator on solid particle (powder material or catalyst) separation and circulating returning, the traditional fluidized bed reactor is designed with a dilute phase zone which occupies 1/2-2/3 of the total height of the reactor and occupies a considerable part of the investment of the reactor.
For example, chinese patent CN111054280B discloses a reaction device and a reaction method for preparing aniline by hydrogenation of multi-zone nitrobenzene, which adopts a plurality of groups of combined devices of two central reaction zones, two downlink zones and three circulation zones, and meanwhile, a sputtering separation member is arranged in a fluidized bed reactor, so that mass transfer and heat transfer in the reactor can be enhanced, deactivation of a catalyst is effectively slowed down, consumption of the catalyst is greatly reduced, and reaction efficiency is improved. However, the reaction device of the utility model is internally provided with a plurality of cyclone separators, the designed dilute phase area occupies a large part of the total height of the reactor, and the dilute phase area adopts an expansion section mode, thus greatly increasing the investment of equipment.
As another example, chinese patent CN109894059B discloses a method for producing (meth) acrylonitrile, which comprises a fluidized bed reactor and a heat exchanger connected to the fluidized bed reactor through a reaction gas outlet pipe, and comprises: introducing a raw material gas into the fluidized bed reactor, and performing an ammoxidation reaction in the presence of a catalyst to obtain a reaction gas; and a step of introducing powder into a reaction gas outlet pipe, and discharging the reaction gas to the heat exchanger while cleaning the heat exchanger, wherein the reaction gas outlet pipe has a first portion extending from the upper portion of the fluidized bed reactor in the height direction of the fluidized bed reactor and reaching the highest point of the reaction gas outlet pipe, and a second portion connected to the highest point and extending to the heat exchanger, and the powder introduction position is a position in the second portion and is lower than the highest point. The reaction device of the utility model is also internally provided with a plurality of cyclone separators, and the designed dilute phase area occupies a large part of the total height of the reactor, thereby greatly increasing the investment of equipment.
If the reactor itself does not have the function of a "separation zone", the gas phase outlet of the reactor must escape the gas containing a large amount of solid particulate material or catalyst, which would result in waste of resources and contamination of the final product if not recycled.
Therefore, it is necessary to provide an automatic circulation and material returning device for a high-temperature pressurized fluidized bed reactor without a dilute phase zone, which can solve the problems of large volume and high cost of the reactor caused by the need of arranging a multi-stage cyclone separator in the fluidized bed reactor in the prior art.
Disclosure of utility model
The utility model aims to provide automatic circulating and returning equipment for a high-temperature pressurized fluidized bed reactor without a dilute phase zone, which can solve the problems of large volume and high cost of the reactor caused by the fact that a multi-stage cyclone separator is arranged in the fluidized bed reactor in the prior art.
The utility model is realized in the following way:
An automatic circulation material returning device for a high-temperature pressurized fluidized bed reactor without a dilute phase zone comprises the high-temperature pressurized fluidized bed reactor without the dilute phase zone, a reactor outlet pipe, a circulation material returning component and a material returning component; the high-temperature pressurized fluidized bed reactor without the dilute phase zone is not provided with the dilute phase zone, one end of a reactor outlet pipe is communicated with a gas outlet of the high-temperature pressurized fluidized bed reactor without the dilute phase zone, a circulating material returning assembly is externally arranged in the high-temperature pressurized fluidized bed reactor without the dilute phase zone, and the other end of the reactor outlet pipe is communicated with an inlet end of the circulating material returning assembly; the outlet end of the circulating return assembly is connected with the feed inlet of the return assembly, and the discharge outlet of the return assembly is communicated with the high-temperature pressurized fluidized bed reactor without dilute phase region.
The circulating and returning assembly comprises a plurality of high-temperature cyclone separation mechanisms with pressure, a conveyor inlet and a monitoring and purging system; the high-temperature high-pressure cyclone separation mechanisms are arranged above the high-temperature high-pressure fluidized bed reactor without a dilute phase zone step by step, the air outlet of the high-temperature high-pressure cyclone separation mechanism at the upper stage is connected with the air inlet of the high-temperature high-pressure cyclone separation mechanism at the lower stage, and the feed opening of the high-temperature high-pressure cyclone separation mechanism at the lower stage is communicated with the feed opening of the high-temperature high-pressure cyclone separation mechanism at the upper stage, so that the high-temperature high-pressure cyclone separation mechanisms are sequentially connected; the other end of the reactor outlet pipe is connected with an air inlet of a first-stage high-temperature cyclone separation mechanism with pressure, a feed opening of the first-stage high-temperature cyclone separation mechanism with pressure is communicated with a feed opening of a return component, and a feed opening of a last-stage high-temperature cyclone separation mechanism with pressure is connected with an inlet of a conveyer; the monitoring and purging system is connected with a plurality of high-temperature pressure cyclone separation mechanisms.
The high-temperature cyclone separation mechanism with pressure at each stage comprises a blanking valve, a material leg and a high-temperature cyclone separator with pressure, wherein a discharge hole of the high-temperature cyclone separator with pressure is communicated with the blanking valve through the material leg, a plurality of measuring points are arranged on the material leg at intervals, and the measuring points are respectively connected to the monitoring and purging system; the air inlet of the first-stage high-temperature cyclone separator with pressure is connected with the other end of the outlet pipe of the reactor, the feed opening of the first-stage blanking valve is communicated with the feed inlet of the return assembly, the air outlet of the upper-stage high-temperature cyclone separator with pressure is communicated with the air inlet of the lower-stage high-temperature cyclone separator with pressure, and the feed opening of the lower-stage blanking valve is connected with the feed opening of the upper-stage blanking valve through a return ball valve by a return connecting pipe to form a return circulation path.
Except the first-stage high-temperature cyclone separation mechanism with pressure, an outer discharge connecting pipe is vertically connected under a discharge hole of the blanking valve, and an outer discharge ball valve is arranged on the outer discharge connecting pipe.
The high-temperature pressure cyclone separator is a single cyclone separator, or comprises a plurality of cyclone separators which are combined in parallel and are arranged in a pressure shell of the separator.
The monitoring and purging system comprises a pressure gauge, a flowmeter, a plurality of stages of central controllers, a pressure transmitter, a monitoring mechanism, a purging mechanism and a check valve; the high-temperature cyclone separation mechanisms with pressure of the multiple stages are respectively and correspondingly connected with the central controllers of the multiple stages, and a plurality of measuring points on the dipleg of the cyclone separation mechanism with pressure of the high-temperature of each stage are respectively and correspondingly connected with a plurality of connecting ends on the central controllers of the corresponding stages; a check valve is connected to each measuring point, and a pressure transmitter is arranged on a pipeline between each measuring point and the connecting end of the central controller; the monitoring mechanism is respectively connected with each measuring point, and the purging mechanism is respectively connected with each measuring point; the multiple-stage central controllers are connected with the monitoring mechanism and the purging mechanism, and a flowmeter and a pressure gauge are arranged on a pipeline connected with the monitoring mechanism.
The monitoring mechanism comprises a low-pressure gas pipeline, a stop valve, a normally open needle valve, a pressure gauge and a flowmeter; the low-pressure gas pipeline is filled with low-pressure gas, the stop valve, the normally open needle valve and the pressure gauge are arranged on the low-pressure gas pipeline, and each measuring point is connected to the low-pressure gas pipeline between the stop valve and the normally open needle valve through the flow gauge;
the purging mechanism comprises a pressure gauge, a normally closed needle valve and a high-pressure gas pipeline; the high-pressure gas pipeline is connected with the check valve and is filled with high-pressure gas, and the pressure gauge and the two normally closed needle valves are respectively arranged on the high-pressure gas pipeline at intervals; the measuring points on the diplegs of the high-temperature and pressure cyclone separating mechanisms are connected with a high-pressure gas pipeline, and the connecting points are positioned between two normally closed needle valves.
When a feed inlet is arranged at the top of the high-temperature pressurized fluidized bed reactor without a dilute phase zone, the feed back component comprises an inner total feed back leg, a total feed back ball valve and an outer total feed back leg; the internal total feed back leg is arranged in the high-temperature pressurized fluidized bed reactor without a dilute phase zone through a plurality of feed leg brackets and is connected with a feed inlet, and an upper end discharge valve, a middle end discharge valve and a tail end discharge valve are sequentially arranged on the internal total feed back leg from top to bottom; the external total feed back leg is arranged outside the high-temperature pressurized fluidized bed reactor without a dilute phase region, the lower end of the external total feed back leg is connected with the feed inlet through the total feed back ball valve, and the upper end of the external total feed back leg is connected with the blanking valve of each stage of high-temperature pressurized cyclone separation mechanism of the circulating feed back assembly.
The upper end discharge valve, the middle end discharge valve and the tail end discharge valve have the same structure and only have different sizes, and the tail end discharge valve comprises a single-head long bolt, a double cone, a nut, a fixed block and a discharge pipe; the fixed block is fixed below the side of the discharge pipe, and the single-head long bolt is adjustably screwed in the fixed block; the double cones are sleeved on the single-head long bolts and locked and fixed through nuts, so that one ends of the double cones are inserted into the discharge pipe;
The double cone comprises a lower cone, a hanging lug and an upper cone; the upper cone is of a positive cone structure, the lower cone is of a reverse cone structure, the upper end of the lower cone is connected with the lower end of the upper cone, and a plurality of hangers are circumferentially uniformly distributed and fixed at the joint of the lower cone and the upper cone; the hangers are sleeved on the single-head long bolts and are locked between the two nuts.
The top of the high-temperature pressurized fluidized bed reactor without the dilute phase zone is not provided with a feed inlet, and the feed back component comprises a reactor feed back inlet, an ejector and an external total dipleg; the reactor feed back opening is obliquely arranged on the side wall of the lower part of the high-temperature pressurized fluidized bed reactor without the dilute phase zone and is communicated with the high-temperature pressurized fluidized bed reactor without the dilute phase zone; one end of the ejector is coaxially connected with the feed back port of the reactor, the other end of the ejector is provided with an air inlet end, one end of the external total material leg is communicated with the ejector near the air inlet end, and the other end of the external total material leg is used as a feed port of the feed back component to be communicated with the feed down ports of the feed down valves of each level.
Compared with the prior art, the utility model has the following beneficial effects:
1. the automatic circulation material returning device is arranged outside the high-temperature pressurized fluidized bed reactor without the dilute phase area, so that the problems of large volume and high cost of the high-temperature pressurized fluidized bed reactor in the prior art are solved, the automatic circulation material returning device is not limited by the internal space of the high-temperature pressurized fluidized bed reactor without the dilute phase area, the system design is more free, three-stage high-temperature pressurized cyclone separators can be used in series, two-stage high-temperature pressurized cyclone separators are used in series or single-stage high-temperature pressurized cyclone separators are used, the comprehensive cost is greatly reduced while the high comprehensive performance is realized, the overhaul and maintenance are also more convenient, and the safety of operators is ensured.
2. According to the utility model, due to the one-stage or multi-stage circulating material returning assembly, part of the side reaction solid products can be conveniently discharged out of the reaction system through the third external discharging connecting pipe or the second external discharging connecting pipe in an on-line manner, so that the impurity content of the automatic circulating material returning to the high-temperature pressurized fluidized bed reactor without a dilute phase zone is greatly reduced, the original higher reaction conversion rate of the reactor can be maintained, and meanwhile, the multi-stage circulating material returning assembly can be used for realizing the purpose of selectively throwing out solid impurities which obstruct the reaction from the high-temperature pressurized fluidized bed reactor without the dilute phase zone by selectively feeding the thermal state granular materials or the catalyst suitable for the main reaction to the most needed position in the reactor, so as to meet the production requirements of different reaction materials.
3. The utility model integrates the traditional multiple groups of cyclone separators which are built in the fluidized bed reactor and connected in parallel in the same stage into the pressure-bearing shell of one separator to form one-stage high-temperature cyclone separator with pressure, and only one dipleg and one blanking valve are arranged at the lower part of the pressure-bearing shell of each separator, thereby greatly simplifying the structure of whole circulating returning material, reducing the number of the blanking valves in multiple, not affecting the cyclone separator with pressure at the upper stage even if one cyclone separator in the pressure-bearing shell of the separator fails, obviously improving the running stability of the whole equipment and being beneficial to reducing the comprehensive manufacturing cost of the fluidized bed reactor.
4. The utility model is provided with the upper end discharge valve, the middle end discharge valve and the tail end discharge valve, so that the internal total feed back leg forms a small fluidized bed, the upper end discharge valve, the middle end discharge valve and the tail end discharge valve are just like balance pipelines, solid particles (powder materials or catalysts) of the internal total feed back leg are respectively discharged into the high-temperature pressurized fluidized bed reactor without a dilute phase zone according to approximate particle size distribution, and the vertical direction 'distributed' circulating feed back mode ensures that the particle size distribution at a return point is relatively uniform, is suitable for different reaction areas, namely the back mixing of the solid particles is greatly reduced, and maintains the reaction conversion rate at a high-efficiency level.
5. The utility model is provided with the monitoring and purging system, the monitoring mechanism can monitor the multistage high-temperature cyclone separation mechanism under pressure in real time, can judge cyclone fault points at any time and process the cyclone fault points in time, and the purging mechanism can purge and dredge multistage diplegs, so that the stability and reliability of automatic circulation and returning are ensured.
6. The traditional fluidized bed reactor is provided with a cyclone system with a plurality of cyclone separators, cyclone diplegs and blanking valves, and the required monitoring mechanism and purging mechanism are complex, and the reliability of failure points is poor. The utility model fully simplifies the monitoring mechanism, the purging mechanism and the process, so that the running stability and reliability of the whole automatic circulation material returning system are obviously improved.
Drawings
FIG. 1 is a schematic diagram of the structure of the automatic recycle return apparatus (three stage, top return) of the present utility model for a high temperature pressurized fluidized bed reactor without dilute phase zone;
FIG. 2 is a piping arrangement diagram of a monitoring and purging system in an automatic cycle return apparatus for a high temperature pressurized fluidized bed reactor without dilute phase zone of the present utility model (three stage, top return);
FIG. 3 is a schematic diagram of the structure of the automatic recycle return apparatus (secondary, top return) of the present utility model for a high temperature pressurized fluidized bed reactor without dilute phase zone;
FIG. 4 is a piping layout (secondary, top return) of the monitoring and purging system of the present utility model for an automatic recycle return apparatus for a high temperature pressurized fluidized bed reactor without dilute phase zone;
FIG. 5 is a schematic diagram of the structure of the automatic recycle return apparatus (first stage, top return) for a freeboard zone high temperature pressurized fluidized bed reactor of the present utility model;
FIG. 6 is a piping arrangement diagram of a monitoring and purging system in an automatic cycle return apparatus for a high temperature pressurized fluidized bed reactor without dilute phase zone of the present utility model (first order, top return);
FIG. 7 is a cross-sectional view of a terminal discharge valve in an automatic recycle return apparatus for a high temperature pressurized fluidized bed reactor without a dilute phase zone according to the present utility model;
FIG. 8 is a cross-sectional view of a double cone in an automatic recycle return apparatus for a high temperature pressurized fluidized bed reactor without a dilute phase zone according to the present utility model;
FIG. 9 is a schematic diagram of the structure of the automatic recycle return apparatus (three stage, side return) for a freeboard zone high temperature pressurized fluidized bed reactor of the present utility model;
FIG. 10 is a schematic diagram of the structure of the automatic recycle return apparatus (secondary, side return) for a freeboard zone high temperature pressurized fluidized bed reactor of the present utility model;
Fig. 11 is a schematic structural view of an automatic circulation and return device (primary, side return) for a high-temperature pressurized fluidized bed reactor without dilute phase zone according to the present utility model.
In the figure, a 1-end discharge valve, a 1001 single-head long bolt, a 1002 double cone, a 10021 lower cone, a 10022 hanging ear, a 10023 upper cone, a 1003 nut, a 1004 fixed block, a 1005 discharge pipe, a 2-freephase area high-temperature pressurized fluidized bed reactor, a 3-middle end discharge valve, a 4-dipleg support, a 5-inner total return leg, a 6-upper end discharge valve, a 7-total return ball valve, an 8-outer total return leg, a 9-reactor outlet pipe, a 10-first blanking valve, a 11-first dipleg, a 12-first monitoring and purging system, a 13-first high-temperature pressurized cyclone, a 14-first outlet pipe, a 15-second high-temperature pressurized cyclone, a 16-third outlet pipe, a 17-second outlet pipe, a 18-third high-temperature pressurized cyclone, a 19-third monitoring and purging system, a second monitoring and purging system 20, a third dipleg, a second dipleg, a third blanking valve 23, a conveying gas inlet 24, a third return ball valve 25, a third discharge ball valve 26, a third discharge pipe 27, a third return pipe 28, a second blanking valve 29, a second return ball valve 30, a second discharge ball valve 31, a second discharge pipe 32, 33 second return connection pipe, 34 reactor return port, 35 ejector, 36 external total dipleg, 101 low-pressure gas pipeline, 102 stop valve, 103 normally open needle valve, 104 manometer, 105 flowmeter, 106 normally closed needle valve, 1071 first central controller, 1072 second central controller, 1073 third central controller, 108 pressure transmitter, 109 check valve, 110 high-pressure gas pipeline.
Detailed Description
The utility model will be further described with reference to the drawings and the specific examples.
Referring to fig. 1, fig. 3, fig. 5, and fig. 9 to fig. 11, an automatic circulation and return device for a high-temperature pressurized fluidized bed reactor without a dilute phase zone comprises a high-temperature pressurized fluidized bed reactor without a dilute phase zone 2, a reactor outlet pipe 9, a circulation and return assembly and a return assembly; the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone is not provided with the dilute phase zone, one end of a reactor outlet pipe 9 is communicated with a gas outlet of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone, a circulating material returning component is arranged outside the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone, and the other end of the reactor outlet pipe 9 is communicated with an inlet end of the circulating material returning component; the outlet end of the circulating return assembly is connected with the feed inlet of the return assembly, and the discharge outlet of the return assembly is communicated with the high-temperature pressurized fluidized bed reactor 2 without dilute phase region.
Referring to fig. 1-6 and 9-11, the recycling and returning assembly includes a plurality of high temperature and pressure cyclone separating mechanisms, a conveyor inlet 24 and a monitoring and purging system; the high-temperature high-pressure cyclone separation mechanisms are arranged above the high-temperature high-pressure fluidized bed reactor 2 without a dilute phase area step by step, the air outlet of the high-temperature high-pressure cyclone separation mechanism at the upper stage is connected with the air inlet of the high-temperature high-pressure cyclone separation mechanism at the lower stage, and the feed opening of the high-temperature high-pressure cyclone separation mechanism at the lower stage is communicated with the feed opening of the high-temperature high-pressure cyclone separation mechanism at the upper stage, so that the high-temperature high-pressure cyclone separation mechanisms are sequentially connected; the stage number of the high-temperature cyclone separation mechanism with pressure can be adaptively adjusted according to actual reaction requirements. The other end of the reactor outlet pipe 9 is connected with an air inlet of a first-stage high-temperature pressurized cyclone separation mechanism (namely, the inlet end of a circulating return assembly), a discharging opening of the first-stage high-temperature pressurized cyclone separation mechanism is communicated with a feeding opening of a return assembly, and a discharging opening of a last-stage high-temperature pressurized cyclone separation mechanism is connected with a conveyor inlet 24; the monitoring and purging system is connected with a plurality of high-temperature pressure cyclone separation mechanisms.
Referring to fig. 1 to 6 and 9 to 11, each stage of the high-temperature cyclone separation mechanism with pressure comprises a blanking valve, a material leg and a high-temperature cyclone separator with pressure, wherein a material outlet of the high-temperature cyclone separator with pressure is communicated with the blanking valve through the material leg, a plurality of measuring points are arranged on the material leg at intervals and are respectively connected to a monitoring and purging system through pipelines; the air inlet of the first-stage high-temperature pressurized cyclone separator is connected with the other end of the reactor outlet pipe 9, the feed opening of the first-stage blanking valve is communicated with the feed inlet of the return assembly, the air outlet of the upper-stage high-temperature pressurized cyclone separator is communicated with the air inlet of the next-stage high-temperature pressurized cyclone separator through the outlet pipe, and the feed opening of the next-stage blanking valve is connected with the feed opening of the upper-stage blanking valve through a return ball valve through a return connecting pipe to form a return circulation path.
Referring to fig. 1, fig. 3, fig. 9 and fig. 10, except for the first-stage high-temperature cyclone separation mechanism with pressure, an outer discharge connecting pipe is vertically connected under a discharge hole of the blanking valve, and an outer discharge ball valve is arranged on the outer discharge connecting pipe.
Referring to fig. 2, 4 and 6, the monitoring and purging system includes a pressure gauge 104, a flow meter 105, a plurality of stage controllers, a pressure transmitter 108, a monitoring mechanism, a purging mechanism and a check valve 109; the high-temperature cyclone separation mechanisms with pressure of the multiple stages are respectively and correspondingly connected with the central controllers of the multiple stages, and a plurality of measuring points on the dipleg of each high-temperature cyclone separation mechanism with pressure of the multiple stages are respectively and correspondingly connected with a plurality of connecting ends on the central controllers of the corresponding stages through pipelines; a check valve 109 is connected to each measuring point, and a pressure transmitter 108 is arranged on a pipeline between each measuring point and the connecting end of the central controller; the monitoring mechanism is respectively connected with each measuring point through a pipeline, and the purging mechanism is respectively connected with each measuring point through a pipeline; the several stages of central controllers are connected with the monitoring mechanism and the purging mechanism, and a flowmeter 105 and a pressure gauge 104 are arranged on the pipeline connecting the several stages of central controllers with the monitoring mechanism.
The check valve 109 is directly connected with each measuring point, so that the gas in the dipleg is prevented from being carried with dust and is led into a pipeline, the pressure value of each measuring point can be taken out in real time, and the working condition of any one-stage high-temperature cyclone separation mechanism with pressure can be confirmed through analysis and comparison of the real-time pressure value of each measuring point.
Referring to fig. 2, 4 and 6, the monitoring mechanism includes a low-pressure gas pipe 101, a stop valve 102, a normally open needle valve 103, a pressure gauge 104 and a flow meter 105; the low-pressure gas pipeline 101 is filled with low-pressure gas, a stop valve 102, a normally open needle valve 103 and a pressure gauge 104 are arranged on the low-pressure gas pipeline 101, and each measuring point is connected to the low-pressure gas pipeline 101 between the stop valve 102 and the normally open needle valve 103 through a pipeline through a flowmeter 105.
The low-pressure gas pipeline 101 can be filled with low-pressure gas such as raw gas or nitrogen, the low-pressure gas in each pipeline has the same gas flow rate by the flowmeter 105, and the gas flow rate can be adaptively adjusted according to actual requirements.
Referring to fig. 2, 4 and 6, the purge mechanism includes a pressure gauge 104, a normally closed needle valve 106 and a high pressure gas pipe 110; the high-pressure gas pipeline 110 is connected with the check valve 109 and is filled with high-pressure gas, and the pressure gauge 104 and the two normally closed needle valves 106 are respectively arranged on the high-pressure gas pipeline 110 at intervals; the measuring points on the diplegs of the high-temperature and pressure cyclone separation mechanisms are connected with the high-pressure gas pipeline 110 through pipelines, and the connecting points are positioned between the two normally-closed needle valves 106.
The high-pressure gas pipeline 110 is filled with high-pressure gas such as raw gas or nitrogen, and the high-pressure gas pipeline 110 is directly connected with the check valve 109, so that if a blockage point of solid particles exists in the corresponding dipleg, the blockage point can be opened by means of the high-pressure gas, and the smoothness of the dipleg is ensured.
Referring to fig. 5, 6 and 11, the circulating and returning assembly preferably comprises a primary high-temperature pressurized cyclone separation mechanism, which comprises a first blanking valve 10, a first dipleg 11 and a first high-temperature pressurized cyclone separator 13; the air inlet of the first high-temperature cyclone separator 13 with pressure is connected with the other end of the reactor outlet pipe 9, the discharge hole of the first high-temperature cyclone separator 13 with pressure is connected with one end of the first dipleg 11, and the other end of the first dipleg 11 is communicated with the feed inlet of the return component through the first blanking valve 10.
This cyclone separation mechanism is pressed to one-level high temperature area corresponds to set up first monitoring and sweeps system 12, because first dipleg 11 is longer pressure conduit, and has certain stock seal height in the normal operating time, consequently set up four measurement points from top to bottom on first dipleg 11: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A. The four measuring points are connected with check valves 109 and are respectively connected with a first-stage central controller 1071 through pipelines, and the four pipelines are respectively provided with a pressure transmitter 108 and a pressure gauge 104. The four measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
Referring to fig. 3, 4 and 10, the circulating return assembly preferably includes a second-stage high-temperature pressure cyclone mechanism including a first blanking valve 10, a first dipleg 11, a first high-temperature pressure cyclone 13, a second outlet pipe 14, a second high-temperature pressure cyclone 15, a second dipleg 22 and a second blanking valve 29. The air inlet of the first high-temperature cyclone separator 13 with pressure is connected with the other end of the reactor outlet pipe 9, the discharge hole of the first high-temperature cyclone separator 13 with pressure is connected with one end of the first dipleg 11, and the other end of the first dipleg 11 is communicated with the feed inlet of the return component through the first blanking valve 10. The gas outlet of the first high-temperature cyclone separator 13 with pressure is connected with the gas inlet of the second high-temperature cyclone separator 15 with pressure through a second outlet pipe 14, the discharge outlet of the second high-temperature cyclone separator 15 with pressure is connected with one end of a second dipleg 22, and the other end of the second dipleg 22 is communicated with the blanking valve of the first blanking valve 10 through a second blanking valve 29 and is communicated with the feed inlet of the return assembly. An outer discharge connecting pipe 32 is vertically connected under the discharge port of the second discharging valve 29 through a second outer discharge ball valve 31.
The second-stage high-temperature pressurized cyclone separation mechanism is correspondingly provided with a first monitoring and purging system 12 and a second monitoring and purging system 20; because the first dipleg 11 and the second dipleg 22 are both longer pressure pipelines, and a certain seal height is arranged in the normal operation, four measuring points are arranged on the first dipleg 11 from top to bottom: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A are arranged on the second dipleg 22 from top to bottom: the first measuring point B, the second measuring point B, the third measuring point B and the fourth measuring point B. The eight measuring points are all connected with a check valve 109, the four measuring points on the first dipleg 11 are respectively connected with a first-stage central controller 1071 through pipelines, the four measuring points on the second dipleg 22 are respectively connected with a second-stage central controller 1072 through pipelines, and the eight pipelines are all provided with a pressure transmitter 108 and a pressure gauge 104. The eight measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and the eight measuring points are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
Referring to fig. 1, 2 and 9, it is preferable that the circulation and return assembly includes a three-stage high temperature pressure cyclone separation mechanism including a first blanking valve 10, a first dipleg 11, a first high temperature pressure cyclone 13, a second outlet pipe 14, a second high temperature pressure cyclone 15, a third outlet pipe 16, a third high temperature pressure cyclone 18, a third dipleg 21, a second dipleg 22, a third blanking valve 23 and a second blanking valve 29. The air inlet of the first high-temperature cyclone separator 13 with pressure is connected with the other end of the reactor outlet pipe 9, the discharge hole of the first high-temperature cyclone separator 13 with pressure is connected with one end of the first dipleg 11, and the other end of the first dipleg 11 is communicated with the feed inlet of the return component through the first blanking valve 10. The gas outlet of the first high-temperature cyclone separator 13 with pressure is connected with the gas inlet of the second high-temperature cyclone separator 15 with pressure through a second outlet pipe 14, the discharge outlet of the second high-temperature cyclone separator 15 with pressure is connected with one end of a second dipleg 22, and the other end of the second dipleg 22 is communicated with the blanking valve of the first blanking valve 10 through a second blanking valve 29 and is communicated with the feed inlet of the return assembly. The air outlet of the second high-temperature cyclone separator 15 with pressure is connected with the air inlet of the third high-temperature cyclone separator 18 with pressure through a third outlet pipe 16, the discharge port of the third high-temperature cyclone separator 18 with pressure is connected with one end of a third dipleg 21, and the other end of the third dipleg 21 is communicated with the discharge port of a second discharge valve 29 through a third discharge valve 23. An outer discharge connecting pipe 32 is vertically connected under the discharge port of the second discharging valve 29 through a second outer discharge ball valve 31; an outer discharge connecting pipe 27 is vertically connected under the discharge hole of the third discharging valve 23 through a third outer discharge ball valve 26.
The three-stage high-temperature pressurized cyclone separation mechanism is correspondingly provided with a first monitoring and purging system 12, a second monitoring and purging system 20 and a third monitoring and purging system 19; because the first dipleg 11, the second dipleg 22 and the third dipleg 21 are all long pressure pipelines, and a certain seal height is arranged in the normal operation, four measuring points are arranged on the first dipleg 11 from top to bottom: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A are arranged on the second dipleg 22 from top to bottom: the first measuring point B, the second measuring point B, the third measuring point B and the fourth measuring point B are arranged on the third dipleg 21 from top to bottom: the first measuring point C, the second measuring point C, the third measuring point C and the fourth measuring point C. The check valves 109 are connected to the 12 measuring points, the four measuring points on the first dipleg 11 are connected with the first-stage central controller 1071 through pipelines respectively, the four measuring points on the second dipleg 22 are connected with the second-stage central controller 1072 through pipelines respectively, the four measuring points on the third dipleg 21 are connected with the third-stage central controller 1073 through pipelines respectively, and the 12 pipelines are provided with the pressure transmitter 108 and the pressure gauge 104. The 12 measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and the 12 measuring points are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
In the recycling and returning assembly, the first high-temperature cyclone separator 13 with pressure, the second high-temperature cyclone separator 15 with pressure and the third high-temperature cyclone separator 18 with pressure can be single cyclone separator in the prior art, or a plurality of (or a plurality of) cyclone separators in the prior art can be combined in parallel and built in a separator pressure-bearing shell, and the cyclone separators can be used as various liners to meet the process requirements when needed. The model specification of the cyclone separator can be adaptively selected according to actual use requirements.
The traditional fluidized bed reactor mostly adopts built-in cyclone mode, when the reactor gas phase throughput is great, often adopt "multiunit multistage" cyclone solution, in order to ensure that every built-in cyclone can all realize stable returning charge, its dipleg lower part all is provided with a whirlwind unloading valve, a cyclone must correspond a whirlwind unloading valve promptly, when whirlwind quantity increases, whirlwind unloading valve's quantity also increases correspondingly, whirlwind unloading valve belongs to vulnerable part and breaks down easily, in case break down can lead to its upper portion whirlwind separator to be out of order entirely, consequently the more the quantity of whirlwind unloading valve the fault point of reaction system also is more, very unfavorable for the long period steady operation of large-scale fluidized bed reactor.
The utility model integrates the 'same-level' cyclone separators (namely parallel cyclone separators) which are originally built in the fluidized bed reactor into the pressure-bearing shell of one separator, thus forming a first-level high-temperature cyclone separator with pressure, and only one dipleg and one blanking valve are arranged at the lower part of the pressure-bearing shell of each separator, thereby greatly simplifying the structure of the whole circulating returning material, reducing the number of the blanking valves in multiple, obviously improving the running stability of the whole equipment and being beneficial to reducing the comprehensive manufacturing cost of the fluidized bed reactor.
Referring to fig. 2, fig. 4 and fig. 6, when a feed inlet is arranged at the top of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, the feed back assembly comprises an inner total feed back leg 5, a total feed back ball valve 7 and an outer total feed back leg 8; the internal total feed back leg 5 is arranged in the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone through a plurality of feed leg brackets 4 and is connected with a feed inlet, and an upper end discharge valve 6, a middle end discharge valve 3 and a tail end discharge valve 1 are sequentially arranged on the internal total feed back leg 5 from top to bottom; the external total feed back leg 8 is arranged outside the high-temperature pressurized fluidized bed reactor 2 without a dilute phase region, the lower end of the external total feed back leg 8 is connected with a feed inlet through the total feed back ball valve 7, and the upper end of the external total feed back leg 8 is connected with the blanking valve of each stage of high-temperature pressurized cyclone separating mechanism of the circulating feed back assembly.
Referring to fig. 5, when the circulating and returning assembly includes a first-stage high-temperature cyclone separating mechanism with pressure, the upper end of the external total returning leg 8 is connected with the discharge port of the first blanking valve 10.
Referring to fig. 3, when the circulating and returning assembly includes a second-stage high-temperature cyclone separation mechanism with pressure, the upper end of the external total returning leg 8 is connected with the discharge port of the first blanking valve 10; the return assembly further comprises a second return ball valve 30, a second outer ball valve 31, a second outer nipple 32 and a second return nipple 33; one end of a second return connecting pipe 33 is connected with the external total return leg 8, the other end of the second return connecting pipe 33 extends obliquely upwards and is coaxially provided with a conveyor inlet 24, the other end of the second return connecting pipe 33 is communicated with a second blanking valve 29, a second return ball valve 30 is arranged on the second return connecting pipe 33, and a second outer connecting pipe 32 is connected below the vertical line of a discharge hole of the second blanking valve 29 through a second outer ball valve 31.
Preferably, the angle between the second return connection 33 and the horizontal is 40 ° -60 °.
Referring to fig. 1, when the circulating and returning assembly includes a three-stage high-temperature cyclone separation mechanism under pressure, the upper end of the external total returning leg 8 is connected with the discharge port of the first blanking valve 10; the return assembly further comprises a third return ball valve 25, a third outer ball valve 26, a third outer nipple 27, a third return nipple 28, a second return ball valve 30, a second outer ball valve 31, a second outer nipple 32, and a second return nipple 33. One end of the second return connecting pipe 33 is connected with the external total return leg 8, the other end of the second return connecting pipe 33 extends obliquely upwards and is coaxially connected with one end of the third return connecting pipe 28, the other end of the second return connecting pipe 33 is communicated with the second discharging valve 29, a second return ball valve 30 is arranged on the second return connecting pipe 33, and the second outer connecting pipe 32 is connected below the vertical line of a discharge hole of the second discharging valve 29 through a second outer ball valve 31. The other end of the third return connecting pipe 28 extends obliquely upwards and is coaxially provided with a conveyer inlet 24, the third return connecting pipe 28 is communicated with the third blanking valve 23, and a third return ball valve 25 is arranged on the third return connecting pipe 28; the third discharge connection 27 is connected below the vertical line of the discharge opening of the third discharge valve 23 by a third discharge ball valve 26.
Preferably, the angle between the third return connection 28 and the horizontal is 40 ° -60 °.
Preferably, the valve cores of the first blanking valve 10, the second blanking valve 29 and the third blanking valve 23 are all arranged in one pressure container, and the valve cores of the first blanking valve 10, the second blanking valve 29 and the third blanking valve 23 adopt one-way valves, so that the requirements of assisting in discharging internal solid particles and blocking the penetration of external gas can be met, and the valve cores can be used as various liners to meet the process requirements when needed.
Although the fluidized bed reactor of part of organic silicon, trichlorosilane and the like can adopt an external multi-stage cyclone material returning mode, the external multi-stage cyclone returns solid particles (powder materials or catalysts) to the fluidized bed reactor through a pneumatic conveying device by a mode of a middle storage tank arranged at the lower part of the external multi-stage cyclone. This return mode belongs to the "intermittent" return mode and requires manual intervention (i.e. non-autonomous automatic continuous mode), but it has the more important drawbacks: the intermittent material returning mode returns the cold solid particles (powder materials or catalysts) into the fluidized bed reactor, and the cold solid particles can not directly participate in the reaction after entering the fluidized bed reactor, and the reaction can only be started after the solid particles are heated to a certain temperature, which is extremely unfavorable for improving the reaction conversion rate of the fluidized bed reactor.
The circulating and returning assembly of the utility model continuously and automatically circulates and returns materials in the reaction process, thereby being capable of directly sending the solid particles in a thermal state into the most needed position of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, and being greatly beneficial to the reaction conversion in the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone.
Referring to fig. 7, the upper end discharge valve 6, the middle end discharge valve 3 and the end discharge valve 1 have the same structure and only have different dimensions, and the structure of the end discharge valve 1 will be described in detail below by taking the example of the end discharge valve 1: the tail end discharge valve 1 comprises a single-head long bolt 1001, a double cone 1002, a nut 1003, a fixed block 1004 and a discharge pipe 1005; the fixed block 1004 is fixed below the side of the discharge pipe 1005, and the single-head long bolt 1001 is adjustably screwed in the fixed block 1004; the double cone 1002 is sleeved on the single-head long bolt 1001 and locked and fixed through the nut 1003, so that one end of the double cone 1002 is inserted into the discharge pipe 1005.
The single-head long bolt 1001, the nut 1003 and the fixed block 1004 form a group of adjustable supporting rods for adjusting the installation position of the double cone 1002 on the discharge pipe 1005, preferably, the adjustable supporting rods can be uniformly distributed in three groups along the circumferential direction of the discharge pipe 1005.
Referring to fig. 8, the double cone 1002 includes a lower cone 10021, a hanging ring 10022 and an upper cone 10023; the upper cone 10023 is of a positive cone structure, the lower cone 10021 is of a reverse cone structure, the upper end of the lower cone 10021 is connected with the lower end of the upper cone 10023, and a plurality of lugs 10022 are circumferentially uniformly distributed and fixed at the connection part of the lower cone 10021 and the upper cone 10023; the lugs 10022 are sleeved on the single-head long bolt 1001 and locked between the two nuts 1003.
Preferably, three lugs 10022 are uniformly circumferentially arranged, such that bipyramid 1002 is adjustably mounted through three lugs 10022 via three sets of adjustable struts.
The nut 1003 can move up and down within the threaded range of the single-head long bolt 1001, so that the opening h (the vertical distance from the bus of the upper cone 10023 to the inner edge of the discharge pipe 1005) of the tail end discharge valve can be adjusted, after the opening h is determined, the double cone 1002 is fixed at the opening through the upper nut 1003 and the lower nut 1003 of the three sets of adjustable supporting rods, so that the tail end discharge valve 1 has the opening adjusting function, namely the tail end discharge valve 1 has the solid particle discharge capacity adjusting function, and the upper end discharge valve 6 and the middle end discharge valve 3 are similar. Preferably, the upper end discharge valve 6 and the middle end discharge valve 3 are smaller in size than the end discharge valve 1, and the discharge capacity of the upper end discharge valve 6 and the middle end discharge valve 3 is smaller than the end discharge valve 1.
Because of the adjustable function of the three discharge valves, a vertical-direction 'distributed' circulating material returning mode can be implemented on the internal total material returning leg 5, the upper end material returning valve 6, the middle end material returning valve 3 and the tail end material returning valve 1 have the same functions as a balance pipeline, and solid particles (powder materials or catalysts) of the internal total material returning leg 5 are respectively discharged into the high-temperature pressurized fluidized bed reactor 2 without a dilute phase area according to approximate particle size distribution, so that the particle size distribution at a returning point is relatively uniform, namely the back mixing of the solid particles is greatly reduced, and the reaction conversion rate is ensured to be at a high-efficiency level.
Preferably, the cone angle α of the upper cone 10023 ranges from 45 ° to 75 °, and the cone angle β of the upper cone 10023 ranges from 100 ° to 130 °. The vertical distance from the inner wall of the lower end of the discharge pipe 1005 to the surface of the double cone 1002 is the opening h of the discharge valve, and the adjustable range of h is 0-95mm. The ratio of the inner diameter d1 of the discharge tube 1005 to the inner diameter d0 of the inner total return leg 5 ranges from d1/d0=0.45 to 1.00; the ratio of the diameter d2 of the junction of the upper end of the lower cone 10021 and the lower end of the upper cone 10023 to the inner diameter d1 of the discharge tube 1005 ranges from d2/d1=1.1 to 1.5.
The solid particles (powder materials or catalysts) in the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone have certain particle size distribution, so that the average particle size of the solid particles (powder materials or catalysts) among each layer of redistribution plates is gradually reduced from bottom to top along the vertical direction, and the particle sizes among the layers of the solid particles are basically consistent due to the homogenization of the redistribution plates. The conventional fluidized bed reactor is basically concentrated and returned to the same height during recycling, so that the particle size of the layer of particles is not uniform, and backmixing is caused, and the backmixing of the particles influences the conversion rate of the reaction to a certain extent.
The utility model arranges the upper end discharge valve 6, the middle end discharge valve 3 and the tail end discharge valve 1 on the internal total feed back 5 of the reactor from top to bottom, so that the internal total feed back 5 forms a small fluidized bed, the upper end discharge valve 6, the middle end discharge valve 3 and the tail end discharge valve 1 are just like balance pipelines, and solid particles (powder materials or catalysts) of the internal total feed back 5 are respectively discharged into the high-temperature pressured fluidized bed reactor 2 in a non-dilute phase area according to approximate particle size distribution, thus the particle size distribution at a return point is relatively uniform, namely the back mixing of the solid particles is greatly reduced, and the reaction conversion rate is maintained at a high-efficiency level.
Referring to fig. 9 to 11, a feed inlet is not formed at the top of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, and the feed back component comprises a reactor feed back port 34, an ejector 35 and an external total dipleg 36; the reactor feed back opening 34 is obliquely arranged on the side wall of the lower part of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone and is communicated with the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone; one end of the ejector 35 is coaxially connected with the reactor feed back port 34, the other end of the ejector 35 is provided with an air inlet end, one end of the external total material leg 36 is communicated with the ejector 35 near the air inlet end, and the other end of the external total material leg 36 is used as a feed port of the feed back component and is communicated with the feed down ports of the various levels of feed down valves.
Due to factors such as process limitation, some high-temperature pressurized fluidized bed reactors 2 without dilute phase areas cannot be returned directly from the top, side return is provided through the reactor return opening 34, and external circulating return of the high-temperature pressurized fluidized bed reactors 2 without dilute phase areas is ensured. The air inlet end is used for being connected with a compressed gas (raw material gas or nitrogen) source, and compressed gas (raw material gas or nitrogen) is introduced into the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone.
Preferably, the included angle between the axial direction of the reactor feed back opening 34 and the horizontal plane is gamma, and the value of gamma is 0-60 degrees.
Referring to fig. 11, when the circulating and returning assembly includes a first-stage high-temperature cyclone separating mechanism with pressure, the upper end of the external total dipleg 36 is connected with the discharge port of the first blanking valve 10.
Referring to fig. 10, when the circulating and returning assembly includes a second-stage high-temperature cyclone separating mechanism with pressure, the upper end of the external total dipleg 36 is connected with the discharge port of the first blanking valve 10; the return assembly further comprises a second return ball valve 30, a second outer ball valve 31, a second outer nipple 32 and a second return nipple 33; one end of the second return connecting pipe 33 is connected with an external total dipleg 36, the other end of the second return connecting pipe 33 extends obliquely upwards and is coaxially provided with a conveyor inlet 24, the other end of the second return connecting pipe 33 is communicated with the second blanking valve 29, the second return connecting pipe 33 is provided with a second return ball valve 30, and the second outer connecting pipe 32 is connected below the vertical line of the discharge hole of the second blanking valve 29 through a second outer ball valve 31.
Referring to fig. 9, when the circulating and returning assembly includes a three-stage high-temperature cyclone separation mechanism with pressure, the upper end of the external total dipleg 36 is connected with the discharge port of the first blanking valve 10; the return assembly further comprises a third return ball valve 25, a third outer ball valve 26, a third outer nipple 27, a third return nipple 28, a second return ball valve 30, a second outer ball valve 31, a second outer nipple 32, and a second return nipple 33. One end of the second return connecting pipe 33 is connected with an external total dipleg 36, the other end of the second return connecting pipe 33 extends obliquely upwards and is coaxially connected with one end of the third return connecting pipe 28, the other end of the second return connecting pipe 33 is communicated with the second discharging valve 29, a second return ball valve 30 is arranged on the second return connecting pipe 33, and the second outer connecting pipe 32 is connected below a vertical line of a discharge hole of the second discharging valve 29 through the second outer ball valve 31. The other end of the third return connecting pipe 28 extends obliquely upwards and is coaxially provided with a conveyer inlet 24, the third return connecting pipe 28 is communicated with the third blanking valve 23, and a third return ball valve 25 is arranged on the third return connecting pipe 28; the third discharge connection 27 is connected below the vertical line of the discharge opening of the third discharge valve 23 by a third discharge ball valve 26.
The high-temperature zone pressure fluidized bed reactor 2 without a dilute phase zone is not provided with the dilute phase zone, so that a high-temperature zone pressure cyclone separation mechanism which is conventionally arranged in the dilute phase zone is moved to the outside of the high-temperature zone pressure fluidized bed reactor 2 without the dilute phase zone, the high-temperature zone pressure fluidized bed reactor 2 without the dilute phase zone only comprises a dense phase zone (concentrated phase section), namely only comprises a reaction zone (or part of a transition zone), and the function of the separation zone is realized by the external automatic circulation material returning device, so that the solid particulate materials or the catalyst contained by the gas phase outlet of the high-temperature zone pressure fluidized bed reactor 2 without the dilute phase zone can be continuously and stably recycled.
Taking a three-stage high-temperature cyclone separation mechanism with pressure as an example, the working process and the working principle of the utility model are as follows:
The gas phase outlet of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone enters a first high-temperature pressurized cyclone separator 13 through a reactor outlet pipe 9, and solid particles are thrown to the wall of the separator under the action of centrifugal force generated by gas rotation, lose inertia after colliding with the wall and fall into an ash bucket at the bottom of the separator under the action of gravity; and the gas is discharged from the first outlet pipe 14 to the second high-temperature pressurized cyclone 15 after being rotated, thereby completing the first separation of the solid particles in the gas phase. If the amount of treated gas is relatively large, the first high-temperature cyclone separator 13 with pressure can be a plurality of (a plurality of) cyclone separators in parallel combination and built in a separator pressure-bearing shell to improve the separator efficiency. The solid particles are captured by the first high-temperature cyclone separator 13 with pressure and then enter the first dipleg 11, and as the first blanking valve 10 has the function of a one-way valve, the opening and closing of the first blanking valve 10 are controlled by the material sealing height of the solid particles in the first dipleg 11, and after the material sealing height of the solid particles in the first dipleg 11 reaches a set value, the first blanking valve 10 is automatically opened and discharges the solid particles in the ash bucket into the external total feed back leg 8 or the external total dipleg 36 through a blanking opening.
After the dust-containing gas enters the second high-temperature cyclone separator 15 with pressure, solid particles are thrown to the wall of the separator under the action of centrifugal force generated by the rotation of the gas, collide with the wall, lose inertia and fall into an ash bucket at the bottom of the separator under the action of gravity; and the gas is discharged from the second outlet pipe 17 to the third high-temperature pressurized cyclone 18 after being rotated, thereby completing the second separation of the solid particles in the gas phase. If the amount of treated gas is relatively large, the second high-temperature cyclone separator 15 with pressure can be a plurality of (a plurality of) cyclone separators in parallel combination and built in a separator pressure-bearing shell to improve the separator efficiency. The solid particles are captured by the second high-temperature cyclone separator 15 with pressure and then enter the second dipleg 22, and as the second blanking valve 29 has the function of a one-way valve, the opening and closing of the second blanking valve 29 are controlled by the material sealing height of the solid particles in the second dipleg 22, and when the material sealing height of the solid particles in the second dipleg 22 reaches a set value, the second blanking valve 29 is automatically opened and discharges the solid particles in the ash bucket into the second material returning connecting pipe 33 or the second outer discharging connecting pipe 32 for returning or discharging.
The dust-containing gas finally enters a third high-temperature cyclone separator 18 with pressure through a second outlet pipe 17, and solid particles are thrown to the wall of the separator under the action of centrifugal force generated by the rotation of the gas, lose inertia after colliding with the wall, fall into an ash bucket under the action of gravity and are discharged outside the separator; and the gas is discharged from the outlet pipe of the third high-temperature pressurized cyclone separator 18 after being rotated, thereby completing the third separation of the solid particles in the gas phase. If the amount of treated gas is relatively large, the third-stage high-temperature cyclone separator 18 with pressure can be a plurality of cyclone separators (a plurality of groups) in parallel combination and built in a separator pressure housing for improving the separator efficiency. The solid particles are captured by the third high-temperature cyclone separator 18 with pressure and then enter the third dipleg 21, and as the third blanking valve 23 has the function of a one-way valve, the opening and closing of the third blanking valve 23 are controlled by the material sealing height of the solid particles in the third dipleg 21, and when the material sealing height of the solid particles in the third dipleg 21 reaches a set value, the third blanking valve 23 is automatically opened and discharges the solid particles in the ash bucket into the third material returning connecting pipe 28 or the third outer discharging connecting pipe 27 for returning or discharging.
And judging whether to return the solid particles subjected to multistage separation to the high-temperature pressurized fluidized bed reactor 2 without the dilute phase or discharge the solid particles outside the high-temperature pressurized fluidized bed reactor 2 without the dilute phase and throw the solid particles out of a reaction system according to the reaction conversion result of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase. When solid particles are discharged, the second discharge ball valve 31 and the third discharge ball valve 26 are opened, the second return ball valve 30 and the third return ball valve 25 are closed, and the solid particles are discharged through the second discharge connecting pipe 32 and the third discharge connecting pipe 27. When returning solid particles to the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, the second outer ball valve 31 and the third outer ball valve 26 are closed, the second return ball valve 30 and the third return ball valve 25 are opened, and the solid particles are converged at the feed opening of the first feed valve 10 through the third return connecting pipe 28 and the second return connecting pipe 33 and enter the external total feed leg 8 or the external total feed leg 36, and then enter the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone.
The high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone is relatively complex, and the reaction materials and the reaction system are quite different, for example, the reactor for synthesizing the organosilicon monomer is a reactor for finally generating the methyl monomer by reacting silicon powder, copper powder and chloromethane gas in the reactor. The reaction is generally carried out at a high temperature of about 280-330℃and a pressure of 0.2-0.6MPa, and a large amount of heat is generated during the reaction. Silicon powder and copper powder materials enter the bottom of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone from a feed inlet, chloromethane gas enters the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone from a chloromethane main pipe on the side surface of the bottom, and high-temperature gas enters the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone from a bottom inlet. The material is blown and pressed upwards from the bottom by the high-temperature pressurized gas at the bottom, the heat is released while the reaction is carried out, and the heat is carried out by the heat conduction oil flowing in the pipeline in the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone. And discharging the solid matters generated by the reaction from a bottom discharge hole, and discharging the generated gas from a top discharge hole. The organosilicon monomer synthesis reaction is extremely complex, and besides the main reaction, a plurality of side reactions exist, and if the side reaction solid products (such as carbon black and the like) cannot be timely discharged from the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, the main reaction can be seriously influenced. Therefore, the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone for synthesizing the organic silicon monomer has limited requirements on the cyclone separation efficiency, namely, the cyclone recovery efficiency is not expected to be too high, otherwise, a large amount of side reaction solid products are continuously accumulated in the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone, and the reaction conversion rate is greatly reduced. But at the same time it is desirable to have as little solids as eventually escape to the subsequent scrubber, otherwise too much sludge is not affordable.
For a reaction system with more side reactions, the reaction conversion rate can be greatly improved by throwing fine impurity solid particles out of the reaction system. Therefore, for the material returning and discharging of the first-stage, second-stage and third-stage high-temperature cyclone separating mechanisms with pressure, the material returning and discharging can be flexibly adjusted according to practical conditions, and the reaction requirements can be met through selective automatic circulation of the material returning, for example: discharging the third-stage high-temperature pressure cyclone separating mechanism, returning the first-stage and second-stage high-temperature pressure cyclone separating mechanisms, discharging the second-stage and third-stage high-temperature pressure cyclone separating mechanisms, returning the first-stage high-temperature pressure cyclone separating mechanisms, and the like.
If the top of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone is provided with a feed inlet, solid particles enter the internal total feed back leg 5 through the external total feed back leg 8 and the total feed back ball valve 7, and then enter the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone through the upper end discharge valve 6, the middle end discharge valve 3 and the tail end discharge valve 1. The internal total feed back leg 5 is also a small fluidized bed in theory, the upper end discharge valve 6, the middle end discharge valve 3 and the tail end discharge valve 1 are like balance pipelines, solid particles (powder materials or catalysts) in the internal total feed back leg 5 are respectively discharged into the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone according to approximate particle size distribution, so that the particle size distribution at a return point is relatively uniform, namely the back mixing of the solid particles is greatly reduced, and the reaction conversion rate is maintained at a high efficiency level.
If the top of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone is provided with a feed inlet, the side wall of the lower part of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone is provided with a reactor feed back opening 34 and is connected with an injection opening 35, and solid particles enter the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone through the injection opening 35 and the reactor feed back opening 34 by an external total dipleg 36.
The first monitoring and purging system 12, the second monitoring and purging system 20 and the third monitoring and purging system 19 are completely identical in operation principle, and the first monitoring and purging system 12 will be described in detail by taking an example:
The first dipleg 11 is provided with four measuring points from top to bottom: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A are respectively connected with a check valve 109, the four measuring points are respectively connected with a first-stage central controller 1071 through pipelines, and the four pipelines are respectively provided with a pressure transmitter 108 and a pressure gauge 104. The four measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
The first monitoring and purging system 12 is functionally divided into two mechanisms: monitoring mechanism and purging mechanism. During normal operation, only the monitoring system works, and during abnormal operation, the monitoring mechanism is closed and switched to the purging mechanism to be used for removing faults. The monitoring mechanism is divided into four routes which respectively correspond to the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A, and low-pressure gas (raw gas or nitrogen) is simultaneously metered by four line flow meters 105, and the four lines all adopt the same gas flow; the four check valves 109 are respectively and directly connected with the four measuring points, so that the gas in the first dipleg 11 is prevented from being carried with dust and is led into the pipeline, and the pressure values of the measuring points are taken out in real time and respectively marked as P1, P2, P3 and P4. With this data, the operation of the first high temperature, pressurized cyclone 13 can be confirmed by analysis and comparison.
The first dipleg 11 is a longer pressure pipeline, and a certain seal height is needed inside during normal operation (the seal surface can be set between the second measuring point a and the third measuring point a), so that the first high-temperature cyclone separator 13 with pressure must meet the following requirements during normal operation: p1=p2 < p3 < p4. If the rule is not satisfied, it can be determined that the corresponding cyclone operation is abnormal. For example, p1=p2 > P3 < P4, which indicates that the pressure at the third measuring point a is higher than that at the second measuring point a and the fourth measuring point a, it may be determined that a blockage phenomenon occurs at the third measuring point a of the first dipleg 11, where the blockage phenomenon may be caused by "bridging" of solid particles in the pipe of the first dipleg 11, and if the first dipleg 11 is not cleaned in time, the first dipleg 11 may be blocked, which eventually results in failure of the first high-temperature pressure cyclone 13.
In order to solve the problem of blockage at the third measuring point a of the first dipleg 11, at this time, all valves of the monitoring mechanism are closed first, and the purging mechanism is switched to the purging mechanism, and the purging mechanism is also divided into four routes corresponding to the first measuring point a, the second measuring point a, the third measuring point a and the fourth measuring point a on the first dipleg 11, and high-pressure gas (raw gas or nitrogen gas) is directly connected with the four non-return valves 109 through the four routes, so that the blockage phenomenon at the third measuring point a of the first dipleg 11 is judged, and the blockage point can be opened by opening the normally closed needle valve 106 on the corresponding pipeline of the purging mechanism.
Example 1:
Referring to fig. 1, an automatic circulation material returning device for a high-temperature pressurized fluidized bed reactor without a dilute phase zone is used for producing aluminum nitride powder products, adopts an aluminum powder direct nitriding method technology, and adopts the following principle: the dried aluminum powder is placed in a high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, and aluminum nitride powder is obtained under the operation conditions of 600-630 ℃ and 3.5 MPa.
The automatic circulating and returning device for the high-temperature pressurized fluidized bed reactor without the dilute phase zone comprises a high-temperature pressurized fluidized bed reactor without the dilute phase zone 2, a reactor outlet pipe 9, a circulating and returning component (three stages) and a returning component; the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone is not provided with the dilute phase zone, one end of a reactor outlet pipe 9 is communicated with a gas outlet of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone, a circulating material returning component is arranged outside the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone, and the other end of the reactor outlet pipe 9 is communicated with an inlet end of the circulating material returning component; the outlet end of the circulating return assembly is connected with the feed inlet of the return assembly, and the discharge outlet of the return assembly is communicated with the high-temperature pressurized fluidized bed reactor 2 without dilute phase region.
The circulation returning charge assembly comprises a three-stage high-temperature pressure cyclone separation mechanism, and the three-stage high-temperature pressure cyclone separation mechanism comprises a first blanking valve 10, a first dipleg 11, a first high-temperature pressure cyclone separator 13, a second outlet pipe 14, a second high-temperature pressure cyclone separator 15, a third outlet pipe 16, a third high-temperature pressure cyclone separator 18, a third dipleg 21, a second dipleg 22, a third blanking valve 23 and a second blanking valve 29. The air inlet of the first high-temperature cyclone separator 13 with pressure is connected with the other end of the reactor outlet pipe 9, the discharge hole of the first high-temperature cyclone separator 13 with pressure is connected with one end of the first dipleg 11, and the other end of the first dipleg 11 is communicated with the feed inlet of the return component through the first blanking valve 10. The gas outlet of the first high-temperature cyclone separator 13 with pressure is connected with the gas inlet of the second high-temperature cyclone separator 15 with pressure through a second outlet pipe 14, the discharge outlet of the second high-temperature cyclone separator 15 with pressure is connected with one end of a second dipleg 22, and the other end of the second dipleg 22 is communicated with the blanking valve of the first blanking valve 10 through a second blanking valve 29 and is communicated with the feed inlet of the return assembly. The air outlet of the second high-temperature cyclone separator 15 with pressure is connected with the air inlet of the third high-temperature cyclone separator 18 with pressure through a third outlet pipe 16, the discharge port of the third high-temperature cyclone separator 18 with pressure is connected with one end of a third dipleg 21, and the other end of the third dipleg 21 is communicated with the discharge port of a second discharge valve 29 through a third discharge valve 23. An outer discharge connecting pipe 32 is vertically connected under the discharge port of the second discharging valve 29 through a second outer discharge ball valve 31; an outer discharge connecting pipe 27 is vertically connected under the discharge hole of the third discharging valve 23 through a third outer discharge ball valve 26.
The three-stage high-temperature pressurized cyclone separation mechanism is correspondingly provided with a first monitoring and purging system 12, a second monitoring and purging system 20 and a third monitoring and purging system 19; because the first dipleg 11, the second dipleg 22 and the third dipleg 21 are all long pressure pipelines, and a certain seal height is arranged in the normal operation, four measuring points are arranged on the first dipleg 11 from top to bottom: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A are arranged on the second dipleg 22 from top to bottom: the first measuring point B, the second measuring point B, the third measuring point B and the fourth measuring point B are arranged on the third dipleg 21 from top to bottom: the first measuring point C, the second measuring point C, the third measuring point C and the fourth measuring point C. The check valves 109 are connected to the 12 measuring points, the four measuring points on the first dipleg 11 are connected with the first-stage central controller 1071 through pipelines respectively, the four measuring points on the second dipleg 22 are connected with the second-stage central controller 1072 through pipelines respectively, the four measuring points on the third dipleg 21 are connected with the third-stage central controller 1073 through pipelines respectively, and the 12 pipelines are provided with the pressure transmitter 108 and the pressure gauge 104. The 12 measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and the 12 measuring points are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
In the recycling and returning assembly, the first high-temperature cyclone separator 13 is built in a separator pressure-bearing shell by adopting the parallel combination of two (or two groups of) cyclone separators in the prior art, and the inner surfaces of the two (or two groups of) cyclone separators are provided with wear-resistant liners for meeting the process requirements. The second high-temperature cyclone separator 15 is built in a separator pressure-bearing shell by adopting four (or four groups of) cyclone separators in parallel connection in the prior art, and the inner surfaces of the four (or four groups of) cyclone separators are provided with wear-resistant liners for meeting the process requirements. The third high-temperature cyclone separator 18 is composed of eight (or eight groups of) cyclone separators in parallel and built in a separator pressure housing in the prior art, and wear-resistant liners are arranged on the inner surfaces of the eight (or eight groups of) cyclone separators to meet the process requirements.
The check valve 109 is directly connected with 12 measuring points, so that gas in the three-stage dipleg can be prevented from being carried with dust and being connected into a pipeline, the pressure values of the 12 measuring points can be taken out in real time, and the working condition of any one-stage high-temperature cyclone separation mechanism with pressure can be confirmed through analysis and comparison of the real-time pressure values of the 12 measuring points.
The monitoring mechanism comprises a low-pressure gas pipeline 101, a stop valve 102, a normally open needle valve 103, a pressure gauge 104 and a flowmeter 105; the low-pressure gas pipeline 101 is filled with low-pressure gas, the stop valve 102, the normally open needle valve 103 and the pressure gauge 104 are arranged on the low-pressure gas pipeline 101, and 12 measuring points are connected to the low-pressure gas pipeline 101 between the stop valve 102 and the normally open needle valve 103 through the pipeline through the flowmeter 105.
The low-pressure gas pipeline 101 can be filled with low-pressure gas such as raw gas or nitrogen, the low-pressure gas in each pipeline has the same gas flow rate by the flowmeter 105, and the gas flow rate can be adaptively adjusted according to actual requirements.
The purge mechanism includes a pressure gauge 104, a normally closed needle valve 106, and a high pressure gas conduit 110; the high-pressure gas pipeline 110 is connected with the check valve 109 and is filled with high-pressure gas, and the pressure gauge 104 and the two normally closed needle valves 106 are respectively arranged on the high-pressure gas pipeline 110 at intervals; the 12 stations are all connected by piping to a high pressure gas piping 110, and the connection point is located between two normally closed needle valves 106.
The high-pressure gas pipeline 110 is filled with high-pressure gas such as raw gas or nitrogen, and the high-pressure gas pipeline 110 is directly connected with the check valve 109, so that if a blockage point of solid particles exists in the corresponding dipleg, the blockage point can be opened by means of the high-pressure gas, and the smoothness of the dipleg is ensured.
The top of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone is provided with a feed inlet, and the feed back component comprises an inner total feed back leg 5, a total feed back ball valve 7 and an outer total feed back leg 8; the internal total feed back leg 5 is arranged in the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone through three feed leg brackets 4 and is connected with a feed inlet, and an upper end discharge valve 6, a middle end discharge valve 3 and a tail end discharge valve 1 are sequentially arranged on the internal total feed back leg 5 from top to bottom; the external total feed back leg 8 is arranged outside the high-temperature pressurized fluidized bed reactor 2 without dilute phase region, and the lower end of the external total feed back leg 8 is connected with the feed inlet through the total feed back ball valve 7.
The upper end of the external total feed back leg 8 is connected with a discharge hole of the first blanking valve 10; the return assembly further comprises a third return ball valve 25, a third outer ball valve 26, a third outer nipple 27, a third return nipple 28, a second return ball valve 30, a second outer ball valve 31, a second outer nipple 32, and a second return nipple 33. One end of the second return connecting pipe 33 is connected with the external total return leg 8, the other end of the second return connecting pipe 33 extends obliquely upwards and is coaxially connected with one end of the third return connecting pipe 28, the other end of the second return connecting pipe 33 is communicated with the second discharging valve 29, a second return ball valve 30 is arranged on the second return connecting pipe 33, and the second outer connecting pipe 32 is connected below the vertical line of a discharge hole of the second discharging valve 29 through a second outer ball valve 31. The other end of the third return connecting pipe 28 extends obliquely upwards and is coaxially provided with a conveyer inlet 24, the third return connecting pipe 28 is communicated with the third blanking valve 23, and a third return ball valve 25 is arranged on the third return connecting pipe 28; the third discharge connection 27 is connected below the vertical line of the discharge opening of the third discharge valve 23 by a third discharge ball valve 26.
The angle between the second return connection 33 and the third return connection 28 and the horizontal is 40.
The valve cores of the first blanking valve 10, the second blanking valve 29 and the third blanking valve 23 are all arranged in a pressure container, the valve cores of the first blanking valve 10, the second blanking valve 29 and the third blanking valve 23 are check valves, the opening and closing of the corresponding check valves are controlled by the material seal heights in the first material leg 11, the second material leg 22 and the third material leg 21 respectively, the requirements of assisting in discharging internal solid particles and blocking the outside air from being in series can be achieved, and in order to meet the process requirements, the wear-resistant lining is arranged on the inner surface of the valve core.
The upper end discharge valve 6, the middle end discharge valve 3 and the tail end discharge valve 1 have the same structure and only have different sizes, and the discharge valves with corresponding sizes can be selected according to actual discharge requirements. The following will describe the structure of the terminal discharge valve 1 in detail by taking it as an example: the end discharge valve 1 comprises a single-head long bolt 1001, a double cone 1002, a nut 1003, a fixed block 1004 and a discharge pipe 1005.
The double cone 1002 includes a lower cone 10021, a hanging ear 10022 and an upper cone 10023; the upper cone 10023 is of a positive cone structure, the lower cone 10021 is of a reverse cone structure, the upper end of the lower cone 10021 is connected with the lower end of the upper cone 10023, and a plurality of hanging lugs 10022 are respectively connected at the connecting positions of the lower cone 10021 and the upper cone 10023 at intervals.
The cone angle α of the upper cone 10023 ranges from 75 ° to 130 °. The vertical distance from the inner wall of the lower end of the discharge pipe 1005 to the surface of the double cone 1002 is the opening h of the discharge valve, and the adjustable range of h is 0-50mm. The ratio of the inner diameter d1 of the discharge tube 1005 to the inner diameter d0 of the inner total return leg 5 ranges from d1/d0=0.45; the ratio of the diameter d2 of the junction of the upper end of the lower cone 10021 and the lower end of the upper cone 10023 to the inner diameter d1 of the discharge tube 1005 ranges from d2/d1=1.1.
The working process and the working principle of the utility model are as follows:
The gas phase outlet of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone enters a first high-temperature pressurized cyclone separator 13 through a reactor outlet pipe 9, and solid particles are thrown to the wall of the separator under the action of centrifugal force generated by gas rotation, lose inertia after colliding with the wall and fall into an ash bucket at the bottom of the separator under the action of gravity; and the gas is discharged from the first outlet pipe 14 to the second high-temperature pressurized cyclone 15 after being rotated, thereby completing the first separation of the solid particles in the gas phase. Because of the relatively large amount of treated gas, the first high-temperature cyclone separator 13 with pressure adopts two (two groups of) cyclone separators which are combined in parallel and are arranged in a pressure-bearing shell of the separator. The solid particles are captured by the first high-temperature cyclone separator 13 with pressure and then enter the first dipleg 11, and as the first blanking valve 10 has the function of a one-way valve, the opening and closing of the first blanking valve 10 are controlled by the material sealing height of the solid particles in the first dipleg 11, and after the material sealing height of the solid particles in the first dipleg 11 reaches a set value, the first blanking valve 10 is automatically opened and discharges the solid particles in the ash bucket into the external total feed back leg 8 or the external total dipleg 36 through a blanking opening.
After the dust-containing gas enters the second high-temperature cyclone separator 15 with pressure, solid particles are thrown to the wall of the separator under the action of centrifugal force generated by the rotation of the gas, collide with the wall, lose inertia and fall into an ash bucket at the bottom of the separator under the action of gravity; and the gas is discharged from the second outlet pipe 17 to the third high-temperature pressurized cyclone 18 after being rotated, thereby completing the second separation of the solid particles in the gas phase. Because of the relatively large amount of treated gas, in order to improve the efficiency of the separator, the second high-temperature cyclone separator 15 with pressure adopts four (four groups of) cyclone separators which are combined in parallel and are built in a pressure-bearing shell of the separator. The solid particles are captured by the second high-temperature cyclone separator 15 with pressure and then enter the second dipleg 22, and as the second blanking valve 29 has the function of a one-way valve, the opening and closing of the second blanking valve 29 are controlled by the material sealing height of the solid particles in the second dipleg 22, and when the material sealing height of the solid particles in the second dipleg 22 reaches a set value, the second blanking valve 29 is automatically opened and discharges the solid particles in the ash bucket into the second material returning connecting pipe 33 or the second outer discharging connecting pipe 32 for returning or discharging.
The dust-containing gas finally enters a third high-temperature cyclone separator 18 with pressure through a second outlet pipe 17, and solid particles are thrown to the wall of the separator under the action of centrifugal force generated by the rotation of the gas, lose inertia after colliding with the wall, fall into an ash bucket under the action of gravity and are discharged outside the separator; and the gas is discharged from the outlet pipe of the third high-temperature pressurized cyclone separator 18 after being rotated, thereby completing the third separation of the solid particles in the gas phase. Because of the relatively large amount of treated gas, the third-stage high-temperature pressurized cyclone separator 18 adopts eight (eight groups of) cyclone separators which are combined in parallel and built in a separator pressure shell. The solid particles are captured by the third high-temperature cyclone separator 18 with pressure and then enter the third dipleg 21, and as the third blanking valve 23 has the function of a one-way valve, the opening and closing of the third blanking valve 23 are controlled by the material sealing height of the solid particles in the third dipleg 21, and when the material sealing height of the solid particles in the third dipleg 21 reaches a set value, the third blanking valve 23 is automatically opened and discharges the solid particles in the ash bucket into the third material returning connecting pipe 28 or the third outer discharging connecting pipe 27 for returning or discharging.
And judging whether to return the solid particles subjected to multistage separation to the high-temperature pressurized fluidized bed reactor 2 without the dilute phase or discharge the solid particles outside the high-temperature pressurized fluidized bed reactor 2 without the dilute phase and throw the solid particles out of a reaction system according to the reaction conversion result of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase. When solid particles are discharged, the second discharge ball valve 31 and the third discharge ball valve 26 are opened, the second return ball valve 30 and the third return ball valve 25 are closed, and the solid particles are discharged through the second discharge connecting pipe 32 and the third discharge connecting pipe 27. When returning solid particles to the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, the second outer ball valve 31 and the third outer ball valve 26 are closed, the second return ball valve 30 and the third return ball valve 25 are opened, and the solid particles are converged at the feed opening of the first feed valve 10 through the third return connecting pipe 28 and the second return connecting pipe 33 and enter the external total feed leg 8 or the external total feed leg 36, and then enter the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone.
For a reaction system with more side reactions, the reaction conversion rate can be greatly improved by throwing fine impurity solid particles out of the reaction system. The material returning and discharging of the first-stage, second-stage and third-stage high-temperature pressure cyclone separating mechanisms can be flexibly adjusted according to actual conditions, such as the material discharging of the third-stage high-temperature pressure cyclone separating mechanism, the material returning of the first-stage and second-stage high-temperature pressure cyclone separating mechanisms, the material discharging of the second-stage and third-stage high-temperature pressure cyclone separating mechanisms, the material returning of the first-stage high-temperature pressure cyclone separating mechanisms and the like.
Solid particles enter the internal total feed back leg 5 through the external total feed back leg 8 and the total feed back ball valve 7, and then enter the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone through the upper end discharge valve 6, the middle end discharge valve 3 and the tail end discharge valve 1. The internal total feed back leg 5 is also a small fluidized bed in theory, the upper end discharge valve 6, the middle end discharge valve 3 and the tail end discharge valve 1 are like balance pipelines, solid particles (powder materials or catalysts) in the internal total feed back leg 5 are respectively discharged into the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone according to approximate particle size distribution, so that the particle size distribution at a return point is relatively uniform, namely the back mixing of the solid particles is greatly reduced, and the reaction conversion rate is maintained at a high efficiency level.
The first monitoring and purging system 12, the second monitoring and purging system 20 and the third monitoring and purging system 19 are completely identical in operation principle, and the first monitoring and purging system 12 will be described in detail by taking an example:
The first dipleg 11 is provided with four measuring points from top to bottom: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A are respectively connected with a check valve 109, the four measuring points are respectively connected with a first-stage central controller 1071 through pipelines, and the four pipelines are respectively provided with a pressure transmitter 108 and a pressure gauge 104. The four measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
The first monitoring and purging system 12 is functionally divided into two mechanisms: monitoring mechanism and purging mechanism. During normal operation, only the monitoring system works, and during abnormal operation, the monitoring mechanism is closed and switched to the purging mechanism to be used for removing faults. The monitoring mechanism is divided into four routes which respectively correspond to the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A, and low-pressure gas (raw gas or nitrogen) is simultaneously metered by four line flow meters 105, and the four lines all adopt the same gas flow; the four check valves 109 are respectively and directly connected with the four measuring points, so that the gas in the first dipleg 11 is prevented from being carried with dust and is led into the pipeline, and the pressure values of the measuring points are taken out in real time and respectively marked as P1, P2, P3 and P4. With this data, the operation of the first high temperature, pressurized cyclone 13 can be confirmed by analysis and comparison.
The first dipleg 11 is a longer pressure pipeline, and a certain seal height is needed inside during normal operation (the seal surface can be set between the second measuring point a and the third measuring point a), so that the first high-temperature cyclone separator 13 with pressure must meet the following requirements during normal operation: p1=p2 < p3 < p4. If the rule is not satisfied, it can be determined that the corresponding cyclone operation is abnormal. For example, p1=p2 > P3 < P4, which indicates that the pressure at the third measuring point a is higher than that at the second measuring point a and the fourth measuring point a, it may be determined that a blockage phenomenon occurs at the third measuring point a of the first dipleg 11, where the blockage phenomenon may be caused by "bridging" of solid particles in the pipe of the first dipleg 11, and if the first dipleg 11 is not cleaned in time, the first dipleg 11 may be blocked, which eventually results in failure of the first high-temperature pressure cyclone 13.
In order to solve the problem of blockage at the third measuring point a of the first dipleg 11, at this time, all valves of the monitoring mechanism are closed first, and the purging mechanism is switched to the purging mechanism, and the purging mechanism is also divided into four routes corresponding to the first measuring point a, the second measuring point a, the third measuring point a and the fourth measuring point a on the first dipleg 11, and high-pressure gas (raw gas or nitrogen gas) is directly connected with the four non-return valves 109 through the four routes, so that the blockage phenomenon at the third measuring point a of the first dipleg 11 is judged, and the blockage point can be opened by opening the normally closed needle valve 106 on the corresponding pipeline of the purging mechanism.
Example 2:
Referring to fig. 1, an automatic circulation material returning device for a high-temperature pressurized fluidized bed reactor without a dilute phase zone is used for producing 10 ten thousand tons of polysilicon products per set of year, and adopts a hydrogenation process, and the principle is as follows: raw materials such as hydrogen, silicon powder, silicon tetrachloride and the like produce trichlorosilane under the conditions of a catalyst and high temperature (550 ℃) and pressure (2.65 MPa).
The automatic circulating and returning device for the high-temperature pressurized fluidized bed reactor without the dilute phase zone comprises a high-temperature pressurized fluidized bed reactor without the dilute phase zone 2, a reactor outlet pipe 9, a circulating and returning component (secondary) and a returning component; the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone is not provided with the dilute phase zone, one end of a reactor outlet pipe 9 is communicated with a gas outlet of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone, a circulating material returning component is arranged outside the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone, and the other end of the reactor outlet pipe 9 is communicated with an inlet end of the circulating material returning component; the outlet end of the circulating return assembly is connected with the feed inlet of the return assembly, and the discharge outlet of the return assembly is communicated with the high-temperature pressurized fluidized bed reactor 2 without dilute phase region.
The circulation returning charge assembly comprises a second-stage high-temperature pressure cyclone separation mechanism, and the second-stage high-temperature pressure cyclone separation mechanism comprises a first blanking valve 10, a first dipleg 11, a first high-temperature pressure cyclone separator 13, a second outlet pipe 14, a second high-temperature pressure cyclone separator 15, a second dipleg 22 and a second blanking valve 29. The air inlet of the first high-temperature cyclone separator 13 with pressure is connected with the other end of the reactor outlet pipe 9, the discharge hole of the first high-temperature cyclone separator 13 with pressure is connected with one end of the first dipleg 11, and the other end of the first dipleg 11 is communicated with the feed inlet of the return component through the first blanking valve 10. The gas outlet of the first high-temperature cyclone separator 13 with pressure is connected with the gas inlet of the second high-temperature cyclone separator 15 with pressure through a second outlet pipe 14, the discharge outlet of the second high-temperature cyclone separator 15 with pressure is connected with one end of a second dipleg 22, and the other end of the second dipleg 22 is communicated with the blanking valve of the first blanking valve 10 through a second blanking valve 29 and is communicated with the feed inlet of the return assembly. An outer discharge connecting pipe 32 is vertically connected under the discharge port of the second discharging valve 29 through a second outer discharge ball valve 31.
The second-stage high-temperature pressurized cyclone separation mechanism is correspondingly provided with a first monitoring and purging system 12 and a second monitoring and purging system 20; because the first dipleg 11 and the second dipleg 22 are both longer pressure pipelines, and a certain seal height is arranged in the normal operation, four measuring points are arranged on the first dipleg 11 from top to bottom: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A are arranged on the second dipleg 22 from top to bottom: the first measuring point B, the second measuring point B, the third measuring point B and the fourth measuring point B. The eight measuring points are all connected with a check valve 109, the four measuring points on the first dipleg 11 are respectively connected with a first-stage central controller 1071 through pipelines, the four measuring points on the second dipleg 22 are respectively connected with a second-stage central controller 1072 through pipelines, and the eight pipelines are all provided with a pressure transmitter 108 and a pressure gauge 104. The eight measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and the eight measuring points are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
In the recycling and returning assembly, the first high-temperature cyclone separator 13 is built in a separator pressure-bearing shell by adopting four (or four groups of) cyclone separators in parallel connection in the prior art, and the inner surfaces of the four (or four groups of) cyclone separators are provided with wear-resistant liners for meeting the process requirements. The second high-temperature cyclone separator 15 is built in a separator pressure-bearing shell by adopting four (or four groups of) cyclone separators in parallel connection in the prior art, and the inner surfaces of the four (or four groups of) cyclone separators are provided with wear-resistant liners for meeting the process requirements.
The check valve 109 is directly connected with 8 measuring points, so that the gas in the secondary dipleg can be respectively prevented from being mixed with dust and is led into a pipeline, the pressure values of the 8 measuring points can be taken out in real time, and the working condition of any one high-temperature cyclone separation mechanism with pressure can be confirmed through analysis and comparison of the real-time pressure values of the 8 measuring points.
The monitoring mechanism comprises a low-pressure gas pipeline 101, a stop valve 102, a normally open needle valve 103, a pressure gauge 104 and a flowmeter 105; the low-pressure gas pipeline 101 is filled with low-pressure gas, the stop valve 102, the normally open needle valve 103 and the pressure gauge 104 are arranged on the low-pressure gas pipeline 101, and 8 measuring points are connected to the low-pressure gas pipeline 101 between the stop valve 102 and the normally open needle valve 103 through the pipeline through the flowmeter 105.
The low-pressure gas pipeline 101 can be filled with low-pressure gas such as raw gas or nitrogen, the low-pressure gas in each pipeline has the same gas flow rate by the flowmeter 105, and the gas flow rate can be adaptively adjusted according to actual requirements.
The purge mechanism includes a pressure gauge 104, a normally closed needle valve 106, and a high pressure gas conduit 110; the high-pressure gas pipeline 110 is connected with the check valve 109 and is filled with high-pressure gas, and the pressure gauge 104 and the two normally closed needle valves 106 are respectively arranged on the high-pressure gas pipeline 110 at intervals; the 8 stations are all connected by piping to a high pressure gas piping 110, and the connection point is located between two normally closed needle valves 106.
The high-pressure gas pipeline 110 is filled with high-pressure gas such as raw gas or nitrogen, and the high-pressure gas pipeline 110 is directly connected with the check valve 109, so that if a blockage point of solid particles exists in the corresponding dipleg, the blockage point can be opened by means of the high-pressure gas, and the smoothness of the dipleg is ensured.
If the top of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone is provided with a feed inlet, the feed back component comprises a reactor feed back port 34, an ejector 35 and an external total dipleg 36. The reactor feed back opening 34 is obliquely arranged on the side wall of the lower part of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone and is communicated with the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone; one end of the ejector 35 is coaxially connected with the reactor feed back port 35, the other end of the ejector 35 is provided with an air inlet end, the air inlet end is externally connected with a compressed gas (raw material gas or nitrogen gas) source, one end of the external total dipleg 36 is communicated with the ejector 35 close to the air inlet end, and the other end of the external total dipleg 36 is used as a feed port of the feed back assembly.
The blanking mouth of the first blanking valve 10 and one end of the second return connecting pipe 33 are connected with the other end of the external total material leg 36, the other end of the second return connecting pipe 33 extends obliquely upwards and is provided with a conveyor inlet 24, the other end of the second return connecting pipe 33 is communicated with the second blanking valve 29, the second return connecting pipe 33 is provided with a second return ball valve 30, and the second outer connecting pipe 32 is connected below the vertical line of the discharging mouth of the second blanking valve 29 through a second outer ball valve 31.
The second outlet pipe 32 is connected below the vertical line of the discharge opening of the second discharge valve 29 by a second outlet ball valve 31.
The included angle between the second return connection pipe 33 and the horizontal plane is 60 degrees; the angle γ between the axis of the reactor feed back 34 and the horizontal plane is 60 °.
The valve cores of the first blanking valve 10 and the second blanking valve 29 are arranged in a pressure container, the valve cores of the first blanking valve 10 and the second blanking valve 29 are check valves, the opening and closing of the corresponding check valves are controlled by the material seal heights in the first material leg 11 and the second material leg 22 respectively, the requirements of assisting in discharging internal solid particles and blocking external gas from being in series can be met, and in order to meet the process requirements, the inner surfaces of the valve cores are provided with wear-resistant liners.
The working process and the working principle of the utility model are as follows:
The gas phase outlet of the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone enters a first high-temperature pressurized cyclone separator 13 through a reactor outlet pipe 9, and solid particles are thrown to the wall of the separator under the action of centrifugal force generated by gas rotation, lose inertia after colliding with the wall and fall into an ash bucket at the bottom of the separator under the action of gravity; and the gas is discharged from the first outlet pipe 14 to the second high-temperature pressurized cyclone 15 after being rotated, thereby completing the first separation of the solid particles in the gas phase. Because of the relatively large amount of treated gas, the first high-temperature cyclone separator 13 with pressure adopts two (two groups of) cyclone separators which are combined in parallel and are arranged in a pressure-bearing shell of the separator. The solid particles are captured by the first high-temperature cyclone separator 13 with pressure and then enter the first dipleg 11, and as the first blanking valve 10 has the function of a one-way valve, the opening and closing of the first blanking valve 10 are controlled by the material sealing height of the solid particles in the first dipleg 11, and after the material sealing height of the solid particles in the first dipleg 11 reaches a set value, the first blanking valve 10 is automatically opened and discharges the solid particles in the ash bucket into the external total feed back leg 8 or the external total dipleg 36 through a blanking opening.
After the dust-containing gas enters the second high-temperature cyclone separator 15 with pressure, solid particles are thrown to the wall of the separator under the action of centrifugal force generated by the rotation of the gas, collide with the wall, lose inertia and fall into an ash bucket at the bottom of the separator under the action of gravity; and the gas is discharged from the second outlet pipe 17 to the third high-temperature pressurized cyclone 18 after being rotated, thereby completing the second separation of the solid particles in the gas phase. Because of the relatively large amount of treated gas, in order to improve the efficiency of the separator, the second high-temperature cyclone separator 15 with pressure adopts four (four groups of) cyclone separators which are combined in parallel and are built in a pressure-bearing shell of the separator. The solid particles are captured by the second high-temperature cyclone separator 15 with pressure and then enter the second dipleg 22, and as the second blanking valve 29 has the function of a one-way valve, the opening and closing of the second blanking valve 29 are controlled by the material sealing height of the solid particles in the second dipleg 22, and when the material sealing height of the solid particles in the second dipleg 22 reaches a set value, the second blanking valve 29 is automatically opened and discharges the solid particles in the ash bucket into the second material returning connecting pipe 33 or the second outer discharging connecting pipe 32 for returning or discharging.
The dust-containing gas finally enters a third high-temperature cyclone separator 18 with pressure through a second outlet pipe 17, and solid particles are thrown to the wall of the separator under the action of centrifugal force generated by the rotation of the gas, lose inertia after colliding with the wall, fall into an ash bucket under the action of gravity and are discharged outside the separator; and the gas is discharged from the outlet pipe of the third high-temperature pressurized cyclone separator 18 after being rotated, thereby completing the third separation of the solid particles in the gas phase. Because of the relatively large amount of treated gas, the third-stage high-temperature pressurized cyclone separator 18 adopts eight (eight groups of) cyclone separators which are combined in parallel and built in a separator pressure shell. The solid particles are captured by the third high-temperature cyclone separator 18 with pressure and then enter the third dipleg 21, and as the third blanking valve 23 has the function of a one-way valve, the opening and closing of the third blanking valve 23 are controlled by the material sealing height of the solid particles in the third dipleg 21, and when the material sealing height of the solid particles in the third dipleg 21 reaches a set value, the third blanking valve 23 is automatically opened and discharges the solid particles in the ash bucket into the third material returning connecting pipe 28 or the third outer discharging connecting pipe 27 for returning or discharging.
And judging whether to return the solid particles subjected to multistage separation to the high-temperature pressurized fluidized bed reactor 2 without the dilute phase or discharge the solid particles outside the high-temperature pressurized fluidized bed reactor 2 without the dilute phase and throw the solid particles out of a reaction system according to the reaction conversion result of the high-temperature pressurized fluidized bed reactor 2 without the dilute phase. When solid particles are discharged, the second discharge ball valve 31 and the third discharge ball valve 26 are opened, the second return ball valve 30 and the third return ball valve 25 are closed, and the solid particles are discharged through the second discharge connecting pipe 32 and the third discharge connecting pipe 27. When returning solid particles to the high-temperature pressurized fluidized bed reactor 2 without a dilute phase zone, the second outer ball valve 31 and the third outer ball valve 26 are closed, the second return ball valve 30 and the third return ball valve 25 are opened, and the solid particles are converged at the feed opening of the first feed valve 10 through the third return connecting pipe 28 and the second return connecting pipe 33 and enter the external total feed leg 8 or the external total feed leg 36, and then enter the high-temperature pressurized fluidized bed reactor 2 without the dilute phase zone.
For a reaction system with more side reactions, the reaction conversion rate can be greatly improved by throwing fine impurity solid particles out of the reaction system. The material returning and discharging of the first-stage and second-stage high-temperature pressure cyclone separating mechanisms can be flexibly adjusted according to actual conditions, such as the material discharging of the second-stage high-temperature pressure cyclone separating mechanism, the material returning of the first-stage high-temperature pressure cyclone separating mechanism, or the simultaneous material returning of the second-stage and first-stage high-temperature pressure cyclone separating mechanisms, etc.
The first monitoring and purging system 12 and the second monitoring and purging system 20 are completely identical in operation principle, and the first monitoring and purging system 12 will be described in detail by taking an example:
The first dipleg 11 is provided with four measuring points from top to bottom: the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A are respectively connected with a check valve 109, the four measuring points are respectively connected with a first-stage central controller 1071 through pipelines, and the four pipelines are respectively provided with a pressure transmitter 108 and a pressure gauge 104. The four measuring points are connected between two normally closed needle valves 106 on a high-pressure gas pipeline 110 of the purging mechanism through pipelines, and are also connected between a stop valve 102 and a normally open needle valve 103 on a low-pressure gas pipeline 101 of the monitoring mechanism through pipelines.
The first monitoring and purging system 12 is functionally divided into two mechanisms: monitoring mechanism and purging mechanism. During normal operation, only the monitoring system works, and during abnormal operation, the monitoring mechanism is closed and switched to the purging mechanism to be used for removing faults. The monitoring mechanism is divided into four routes which respectively correspond to the first measuring point A, the second measuring point A, the third measuring point A and the fourth measuring point A, and low-pressure gas (raw gas or nitrogen) is simultaneously metered by four line flow meters 105, and the four lines all adopt the same gas flow; the four check valves 109 are respectively and directly connected with the four measuring points, so that the gas in the first dipleg 11 is prevented from being carried with dust and is led into the pipeline, and the pressure values of the measuring points are taken out in real time and respectively marked as P1, P2, P3 and P4. With this data, the operation of the first high temperature, pressurized cyclone 13 can be confirmed by analysis and comparison.
The first dipleg 11 is a longer pressure pipeline, and a certain seal height is needed inside during normal operation (the seal surface can be set between the second measuring point a and the third measuring point a), so that the first high-temperature cyclone separator 13 with pressure must meet the following requirements during normal operation: p1=p2 < p3 < p4. If the rule is not satisfied, it can be determined that the corresponding cyclone operation is abnormal. For example, p1=p2 > P3 < P4, which indicates that the pressure at the third measuring point a is higher than that at the second measuring point a and the fourth measuring point a, it may be determined that a blockage phenomenon occurs at the third measuring point a of the first dipleg 11, where the blockage phenomenon may be caused by "bridging" of solid particles in the pipe of the first dipleg 11, and if the first dipleg 11 is not cleaned in time, the first dipleg 11 may be blocked, which eventually results in failure of the first high-temperature pressure cyclone 13.
In order to solve the problem of blockage at the third measuring point a of the first dipleg 11, at this time, all valves of the monitoring mechanism are closed first, and the purging mechanism is switched to the purging mechanism, and the purging mechanism is also divided into four routes corresponding to the first measuring point a, the second measuring point a, the third measuring point a and the fourth measuring point a on the first dipleg 11, and high-pressure gas (raw gas or nitrogen gas) is directly connected with the four non-return valves 109 through the four routes, so that the blockage phenomenon at the third measuring point a of the first dipleg 11 is judged, and the blockage point can be opened by opening the normally closed needle valve 106 on the corresponding pipeline of the purging mechanism.
The foregoing description of the preferred embodiments of the utility model is not intended to limit the scope of the utility model, and therefore, any modifications, equivalents, improvements, etc. that fall within the spirit and principles of the utility model are intended to be included within the scope of the utility model.
Claims (10)
1. An automatic circulation material returning device for a high-temperature pressurized fluidized bed reactor without a dilute phase zone, which is characterized in that: comprises a high-temperature pressurized fluidized bed reactor (2) without a dilute phase zone, a reactor outlet pipe (9), a circulating material returning component and a material returning component; a dilute phase zone is not arranged in the high-temperature pressurized fluidized bed reactor (2) without the dilute phase zone, one end of a reactor outlet pipe (9) is communicated with a gas outlet of the high-temperature pressurized fluidized bed reactor (2) without the dilute phase zone, a circulating material returning component is arranged outside the high-temperature pressurized fluidized bed reactor (2) without the dilute phase zone, and the other end of the reactor outlet pipe (9) is communicated with an inlet end of the circulating material returning component; the outlet end of the circulating return component is connected with the feed inlet of the return component, and the discharge outlet of the return component is communicated with the high-temperature pressurized fluidized bed reactor (2) without dilute phase region.
2. The automatic circulation and return device for a high temperature pressurized fluidized bed reactor without dilute phase zone according to claim 1, characterized in that: the circulating and returning assembly comprises a plurality of high-temperature cyclone separation mechanisms with pressure, a conveyor inlet (24) and a monitoring and purging system; the high-temperature high-pressure cyclone separation mechanisms are arranged above the high-temperature high-pressure fluidized bed reactor (2) without a dilute phase area step by step, the air outlet of the high-temperature high-pressure cyclone separation mechanism at the upper stage is connected with the air inlet of the high-temperature high-pressure cyclone separation mechanism at the lower stage, and the feed opening of the high-temperature high-pressure cyclone separation mechanism at the lower stage is communicated with the feed opening of the high-temperature high-pressure cyclone separation mechanism at the upper stage, so that the high-temperature high-pressure cyclone separation mechanisms at the lower stage are sequentially connected; the other end of the reactor outlet pipe (9) is connected with an air inlet of a first-stage high-temperature cyclone separation mechanism with pressure, a feed opening of the first-stage high-temperature cyclone separation mechanism with pressure is communicated with a feed opening of a return component, and a feed opening of the last-stage high-temperature cyclone separation mechanism with pressure is connected with a conveyor inlet (24); the monitoring and purging system is connected with a plurality of high-temperature pressure cyclone separation mechanisms.
3. An automatic circulation return device for a freeboard high temperature pressurized fluidized bed reactor according to claim 2, characterized in that: the high-temperature cyclone separation mechanism with pressure at each stage comprises a blanking valve, a material leg and a high-temperature cyclone separator with pressure, wherein a discharge hole of the high-temperature cyclone separator with pressure is communicated with the blanking valve through the material leg, a plurality of measuring points are arranged on the material leg at intervals, and the measuring points are respectively connected to the monitoring and purging system; the air inlet of the first-stage high-temperature cyclone separator with pressure is connected with the other end of the reactor outlet pipe (9), the feed opening of the first-stage blanking valve is communicated with the feed inlet of the return component, the air outlet of the upper-stage high-temperature cyclone separator with pressure is communicated with the air inlet of the next-stage high-temperature cyclone separator with pressure, and the feed opening of the next-stage blanking valve is connected with the feed opening of the upper-stage blanking valve through a return ball valve by a return connecting pipe to form a return circulation path.
4. An automatic circulation return device for a freeboard high temperature pressurized fluidized bed reactor according to claim 3, characterized by: except the first-stage high-temperature cyclone separation mechanism with pressure, an outer discharge connecting pipe is vertically connected under a discharge hole of the blanking valve, and an outer discharge ball valve is arranged on the outer discharge connecting pipe.
5. An automatic circulation return device for a freeboard high temperature pressurized fluidized bed reactor according to claim 3, characterized by: the high-temperature pressure cyclone separator is a single cyclone separator, or comprises a plurality of cyclone separators which are combined in parallel and are arranged in a pressure shell of the separator.
6. An automatic circulation return device for a freeboard high temperature pressurized fluidized bed reactor according to claim 2, characterized in that: the monitoring and purging system comprises a pressure gauge (104), a flowmeter (105), a plurality of stages of central controllers, a pressure transmitter (108), a monitoring mechanism, a purging mechanism and a check valve (109); the high-temperature cyclone separation mechanisms with pressure of the multiple stages are respectively and correspondingly connected with the central controllers of the multiple stages, and a plurality of measuring points on the dipleg of the cyclone separation mechanism with pressure of the high-temperature of each stage are respectively and correspondingly connected with a plurality of connecting ends on the central controllers of the corresponding stages; a check valve (109) is connected to each measuring point, and a pressure transmitter (108) is arranged on a pipeline between each measuring point and the connecting end of the central controller; the monitoring mechanism is respectively connected with each measuring point, and the purging mechanism is respectively connected with each measuring point; the plurality of stages of central controllers are connected with the monitoring mechanism and the purging mechanism, and a flowmeter (105) and a pressure gauge (104) are arranged on a pipeline connected with the monitoring mechanism.
7. The automatic circulation and return device for a freeboard high-temperature pressurized fluidized bed reactor according to claim 6, wherein: the monitoring mechanism comprises a low-pressure gas pipeline (101), a stop valve (102), a normally open needle valve (103), a pressure gauge (104) and a flowmeter (105); the low-pressure gas pipeline (101) is filled with low-pressure gas, the stop valve (102), the normally open needle valve (103) and the pressure gauge (104) are arranged on the low-pressure gas pipeline (101), and each measuring point is connected to the low-pressure gas pipeline (101) between the stop valve (102) and the normally open needle valve (103) through the flowmeter (105);
The purging mechanism comprises a pressure gauge (104), a normally closed needle valve (106) and a high-pressure gas pipeline (110); the high-pressure gas pipeline (110) is connected with the check valve (109) and is filled with high-pressure gas, and the pressure gauge (104) and the two normally closed needle valves (106) are respectively arranged on the high-pressure gas pipeline (110) at intervals; the measuring points on the diplegs of the high-temperature and pressure cyclone separation mechanisms are connected with a high-pressure gas pipeline (110), and the connecting points are positioned between two normally closed needle valves (106).
8. The automatic circulation and return device for a high temperature pressurized fluidized bed reactor without dilute phase zone according to claim 1, characterized in that: when a feed inlet is arranged at the top of the high-temperature pressurized fluidized bed reactor (2) without a dilute phase zone, the feed back component comprises an inner total feed back leg (5), a total feed back ball valve (7) and an outer total feed back leg (8); the internal total feed back leg (5) is arranged in the high-temperature pressurized fluidized bed reactor (2) without a dilute phase zone through a plurality of feed back leg brackets (4) and is connected with a feed inlet, and an upper end discharge valve (6), a middle end discharge valve (3) and a tail end discharge valve (1) are sequentially arranged on the internal total feed back leg (5) from top to bottom; the external total feed back leg (8) is arranged outside the high-temperature pressurized fluidized bed reactor (2) without a dilute phase region, the lower end of the external total feed back leg (8) is connected with the feed inlet through the total feed back ball valve (7), and the upper end of the external total feed back leg (8) is connected with the feed down valve of each stage of high-temperature pressurized cyclone separation mechanism of the circulating feed back assembly.
9. The automatic circulation and return device for a freeboard high-temperature pressurized fluidized bed reactor according to claim 8, characterized in that: the upper end discharge valve (6), the middle end discharge valve (3) and the tail end discharge valve (1) are identical in structure and only different in size, and the tail end discharge valve (1) comprises a single-head long bolt (1001), a double cone (1002), a nut (1003), a fixed block (1004) and a discharge pipe (1005); the fixed block (1004) is fixed below the side of the discharge pipe (1005), and the single-head long bolt (1001) is adjustably screwed in the fixed block (1004); the double cone (1002) is sleeved on the single-head long bolt (1001) and locked and fixed through the nut (1003), so that one end of the double cone (1002) is inserted into the discharge pipe (1005);
The double cone (1002) comprises a lower cone (10021), a hanging lug (10022) and an upper cone (10023); the upper cone (10023) is of a positive cone structure, the lower cone (10021) is of a reverse cone structure, the upper end of the lower cone (10021) is connected with the lower end of the upper cone (10023), and a plurality of lugs (10022) are circumferentially uniformly distributed and fixed at the joint of the lower cone (10021) and the upper cone (10023); the hanging lugs (10022) are sleeved on the single-head long bolt (1001) and are locked between the two nuts (1003).
10. The automatic circulation and return device for a high temperature pressurized fluidized bed reactor without dilute phase zone according to claim 1, characterized in that: the top of the high-temperature pressurized fluidized bed reactor (2) without a dilute phase zone is not provided with a feed inlet, and the feed back component comprises a reactor feed back opening (34), an ejector (35) and an external total dipleg (36); the reactor feed back opening (34) is obliquely arranged on the side wall of the lower part of the high-temperature pressurized fluidized bed reactor (2) without the dilute phase zone and is communicated with the high-temperature pressurized fluidized bed reactor (2) without the dilute phase zone; one end of the ejector (35) is coaxially connected with the reactor feed back opening (34), the other end of the ejector (35) is provided with an air inlet end, one end of the external total material leg (36) is communicated with the ejector (35) close to the air inlet end, and the other end of the external total material leg (36) is used as a feed inlet of the feed back assembly to be communicated with the feed down opening of each stage of feed down valve.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323082526.2U CN221182712U (en) | 2023-11-15 | 2023-11-15 | Automatic circulation material returning device for high-temperature pressurized fluidized bed reactor without dilute phase zone |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323082526.2U CN221182712U (en) | 2023-11-15 | 2023-11-15 | Automatic circulation material returning device for high-temperature pressurized fluidized bed reactor without dilute phase zone |
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| CN202323082526.2U Active CN221182712U (en) | 2023-11-15 | 2023-11-15 | Automatic circulation material returning device for high-temperature pressurized fluidized bed reactor without dilute phase zone |
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