RU88662U1 - DEVICE FOR PRODUCING RAW MATERIALS FOR THE PRODUCTION OF CALCIUM CARBIDE - Google Patents

Abstract

A device for producing raw materials for the production of calcium carbide, containing a two-chamber mixer connected to the semi-coke and lime hoppers with batchers, and a semi-coke cooling system with semi-coking gases, as well as a vertical cylindrical dust concentrator for the thermal processing of oxidized brown coal, connected to the indicated semi-coke bunker, having axial and tangential upper and lower inlet nozzles, discharge pipe and tangential branch pipes for the discharge of the concentrated mixture, separated by a transverse separation a rod to the upper and lower sections, communicating with a bypass pipe, at the ends of which there are upper and lower reversible blade swirls, between which are located the upper and lower inlet nozzles connected by a dust collector with a gate through a dust pipe with a dust hopper, and a fuel oil nozzle is placed in the axial inlet pipe and an air nozzle, while the branch pipes of the concentrated mixture of the dust concentrator are connected to the semicoke bunker, and additional swirlers, characterized in that the additional Numerous swirls are installed together with the inlet nozzles in the lower section of the dust concentrator, between the lower end blade vortex swirl and the transverse baffle, with the blades tilted in the same direction as the blades of the lower end swirl reverser, with a pitch between swirls equal to the cross-sectional height of the lower dust plume inlet tangential nozzles, and the overflow pipe is perforated with holes located between the swirlers, and at the transverse partition, made in half of the housing

Description

The technical solution relates to the chemical industry, in particular to the production of calcium carbide, and can be used to obtain calcium carbide used in the production of acetylene.

A device for producing raw materials for the production of calcium carbide from the coke ash residue of the thermal processing of oxidized brown coals with the content of calcium oxide in the coke residue is 47.5%, and carbon 35.4% from the method of producing calcium carbide by high-temperature smelting it in the presence of calcium carbonate up to 28 , 3% in the form of limestone by weight of the mixture (RF patent No. 2129093, IPC СВВ 31/32, 1999). The disadvantage of this device is the need to use calcium carbonate to correct the composition of the charge, which increases the cost of the process.

A device for producing raw materials for the production of calcium carbide is known, comprising a twin-shaft mixer connected to semi-coke and lime hoppers with dispensers, and a semi-coke cooling system with semi-coking gases containing carbon dioxide (USSR copyright certificate No. 276925, IPC СВВ 31/32, 1970). The disadvantage is the low productivity of the installation due to the long cooling of the semi-coke.

It is also known a device for producing raw materials for the production of calcium carbide, containing a semi-coke bunker with a system for the thermal processing of oxidized brown coal connected to a semi-coke bunker consisting of a vertical cylindrical dust concentrator having axial and tangential upper and lower inlet pipes, a waste pipe and tangential branch pipes for concentrated mixture, divided by a transverse partition into upper and lower sections, communicating bypass pipe, at the ends of which is installed the upper and lower reversible blade swirls, between which the indicated inlet pipes are located, connected by a dust collector with a gate through a dust pipe with a dust hopper, and a fuel oil nozzle and an air nozzle are placed in the inlet axial pipe, one of the pipes of the concentrated mixture discharge to the dust concentrator is connected to semi-coke bunker (RF patent No. 2088851, IPC F23K 1/00, 1997)

A disadvantage of the known device is its low productivity, low temperature and shallow semi-coking depth, which do not provide the optimal stoichiometric ratio of charge components in the production of calcium carbide.

The basis of the proposed solution is the task of increasing the productivity, temperature and depth of semi-coking to ensure the optimal stoichiometric ratio of the components of the mixture in the production of calcium carbide.

The problem is solved in that in a device for producing raw materials for the production of calcium carbide, containing a twin-shaft mixer connected to semi-coke and lime hoppers with batchers, and a semi-coke cooling system with semi-coking gases, as well as a vertical cylindrical dust concentrator for the thermal processing of oxidized brown coal, connected to the specified a semi-coke bunker having axial and tangential upper and lower inlet nozzles, a discharge pipe and tangential branch pipes of a concentrated mixture outlet, section equipped with a transverse baffle on the upper and lower sections, communicating bypass pipe, at the ends of which are installed the upper and lower reversible blade swirls, between which the upper and lower inlet pipes are connected, connected by a dust collector with a gate through a dust pipe with a dust hopper, and an ignition tube is located in the axial inlet pipe a fuel oil nozzle and an air nozzle, while the branch pipes for the removal of the concentrated mixture of the dust concentrator are connected to the semi-coke bunker, and additional swirlers, agree of the invention, additional swirls are installed together with the inlet pipes in the lower section of the dust concentrator between the lower end blade swirl and the transverse partition with the blades inclined in the same direction as the blades of the lower end swirl, with a pitch between swirls equal to the cross-sectional height of the dust plume lower tangential inlet nozzles, and the overflow pipe is perforated with holes located between the swirlers, and at the transverse partition made in half of the dust concentrator body, free of inlet pipes, and the outlet section of the bypass pipe is placed inside the dust pipe of the dust concentrator, with the formation of an annular gap between them, and connected to the lime hopper, while one of the pipes of the concentrated mixture discharge is installed under the transverse partition.

The drawing shows the proposed device for the production of raw materials for the production of calcium carbide, which contains a twin-shaft mixer 1 connected to the bunkers 2 of semi-coke and 3 lime with batchers 4 and 5, respectively, and the cooling system of the semi-coke by semi-coking gases, as well as a vertical cylindrical dust concentrator 6 to obtain semi-coke having axial 7 and tangential upper 8 and lower 9 inlet nozzles, a waste pipe 10, as well as tangential nozzles 11 and 12 of the outlet of the concentrated mixture. The dust concentrator 6 is divided by a transverse partition 13 into the upper 14 and lower 15 sections, communicating with each other bypass pipe 16, at the ends of which are installed the upper 17 and lower 18 end reversible blade swirls. These tangential upper and lower inlet nozzles 8 and 9 are made respectively of smaller and larger diameters, are installed between swirlers under each other and are connected by a dust collector 19 with a gate 20 through a dust pipe 21 with a dust hopper 22 with a feeder 23. And in the axial inlet 7 there is a fuel oil the nozzle 24 and the air nozzle 25, while the nozzles 11 and 12 of the outlet of the concentrated mixture of the dust concentrator 6 are tangential and connected to the hopper of the semi-coke 2 through a cyclone 26. The branch pipe 11 of the outlet is concentrated of the mixture is located on the housing of the dust concentrator 6 under the transverse partition 13. Additional swirls 27 and 28 are installed together with the inlet pipes 8 and 9 in the lower section 15 of the dust concentrator 6, between the lower end blade vortex swirl 18 and the transverse partition 13 with the blades tilted in the same direction, as the blades of the lower end reversing swirler, 18. The blades in the swirls are overlapped with a small angle of inclination and narrow slots between the blades. The swirl 28 may have a tilt of the blades in the opposite direction to prevent large uncrocked dust from entering the outlet pipe 11 of the concentrated mixture. The step between the swirls of the lower section 15 of the dust concentrator is equal to the cross-sectional height of the dust flares of the lower tangential inlet pipes 9. The bypass pipe 16 is perforated with holes 29 located between the swirls and at the transverse partition 13 made in half of the housing of the dust concentrator 6, free from inlet pipes 8 and 9 The output section 30 of the bypass pipe 16 is placed inside the waste pipe 10 of the dust concentrator with the formation of an annular gap 31 between them and is connected to the lime hopper 3 through a cyclone 32, Brosno pipe 33 which is connected to the "suction" fan 34, the discharge port of which is connected to the ejector 35, both connected through gate 36 to a source 37 of hot air. The exhaust pipe 10 of the dust concentrator is connected to a cyclone 38 connected to a semi-coke hopper 2 with a dispenser 4. The inlet tangential nozzles (not indicated) of the cyclones 26, 32 and 38 are connected to the pipes 39 for supplying cooled semi-coking gases containing carbon dioxide. The device may also contain an additional kindling hopper 40 of a semicoke with a feeder 41 connected to an ejector 42 connected to the discharge pipe of the fan 43 connected to the discharge pipe 44 of the cyclone 26. The passive nozzle of the ejector 42 is connected to the axial inlet pipe 7 of the dust concentrator. The dust pipe 21 contains a gate 45, and a twin-shaft mixer 1 - a finished charge hopper 46 for producing calcium carbide with a dispenser 47. Between the inlet pipe 7 and the bypass pipe 16 there is an annular gap 48 for the passage of gases. The pipes 49 for the selection of semi-coking gases from the discharge pipes 33 and 44 of the cyclones 32 and 26 through the cooler 50 are connected to the tangential pipes 39 for supplying the semi-coking gases to the inlet pipes (not indicated) of the cyclones 26.32 and 38 for cooling the charge. The housing of the dust concentrator 6 and the bypass pipe 16 can be made in the form of muffles, and swirlers made of alloy steel.

The inventive device operates as follows. With the gate 45 open and the gate 36 closed, the fans 34 and 43 are turned on and the entire device is blown. Then the ignition fuel oil nozzle 24 is turned on and the muffle of the bypass pipe 16 is heated. After that, from the ignition hopper 40, in the ignition mode, the feeder 41, through the ejector 42, feeds into the axial inlet nozzle 7 semi-coke, which flashes when it comes into contact with the torch of the ignition oil nozzle 24 and burns out in the muffle of the bypass pipe 16. After heating the muffle of the bypass pipe 16, the gate 45 closes, and the gate 36 opens and high-concentration dust is supplied with primary air from the hopper 22 by the feeder 23 using a core 35, operating from a hot air source 36 and from semi-coking gases supplied by a fan 34, to the upper section 14 of the dust concentrator 6. In this case, the dust supply to the lower tangential inlet pipe 9 of the upper section 14 of the dust concentrator is blocked by the gate 20. Dust from the upper inlet pipe 8, in contact with the hot muffle of the bypass pipe 16, flashes and cokes due to the primary air. The reversing swirler 17 prevents the passage of coarse non-coking dust through the annular gap 48 into the bypass pipe 16, as a result of which a finely dispersed semi-coke with a developed combustion surface enters the bypass pipe, and the gas ballast is removed through an opening 29 in the bypass pipe 16, above the transverse partition 13, and through the annular gap 48, passing between the blades of the swirl 17 in the opposite direction of dust rotation. Then, the gate 20 opens the entrance to the lower inlet pipe 9, and the amount of dust increases with the help of the feeder 23 supplied through the pipes 8 and 9 to the upper section 14 of the dust concentrator. After combustion stabilization in the upper section 14 of the dust concentrator and the bypass pipe 16, the gate 45 opens, and the revolutions of the feeder 23 are added, and the dust enters the inlet pipes 9 of the lower section 15 of the dust concentrator when the upper pipes 8 of the lower section 15 of the dust concentrator are closed by 20 gates. The dust entering the lower section of the dust concentrator is coked by primary air, in which low-calorie products of thermal degradation of coal are burned out, and the coke base remains through reversible swirlers 18 and 28, which prevent the removal of uncoking dust, the semi-coke enters the nozzles 11 and 12 of the concentrated mixture, and then through cyclone 26 to the semi-coke hopper 2. Simultaneously with the semicoke, in the inlet pipe of the cyclone 26 from the pipe 39, cold coking gases are taken through the cooler 50, taken from the waste pipes 33 and 44 after the fans 34 and 43, which provide cooling of the semicoke and its saturation with carbon dioxide during the rotation of the semicoke in cyclones 26.32 and 38. The continuous process does not require additional cooling time, which increases the productivity of the device. After the device returns to normal operation, the semi-coke feeder 41 is disconnected from the ignition hopper 40 and the ignition oil nozzle 24. The coking in the lower section of the dust concentrator is carried out through a hot bypass pipe 16. due to the additional fuel supplied to the upper section of the dust concentrator. which increases the percentage of carbon in the semi-coke collected in the hopper 2. This ensures the optimal stoichiometric ratio of the components of the charge. When dust is supplied to the upper inlet pipes 8, by opening them with a gate 20, the dust torch emerging from these pipes is cut off by the opposite ends of the blades of the upper swirls 27, since the installation step of the swirls in the lower section is equal to the cross-sectional height of the dust flames of the lower inlet pipes 9, and the dust jet from the inlet pipes 8 exceeds this distance between the swirls, and the dust will go up between the swirl blades, preventing the fuel from falling down, which increases the coking time. When dust is coked in the upper and lower sections of the dust concentrator, the fly ash and semi-coking gases will go through openings 29 to cyclone 32, where the fly ash containing calcium oxide will remain in hopper 3, and the gases, after cooling, by the addition of cold gases from pipe 39, will go through the fan 34 to the ejector 35 to supply dust for coking. Part of the gases through the sampling pipe 49 will return to the inlet of the cyclone 32 after cooling them in the cooler 50. The gases contain a significant percentage of carbon dioxide, which increases the yield of calcium carbide. Samples for analysis of carbon and calcium content are taken from bins 2 and 3, according to which the components of the mixture are dosed through batchers 4 and 5 into a twin-roll mixer 1, after which the finished mixture enters the bunker 46 with batcher 47, from which the carbide is dosed calcium in a furnace for producing calcium carbide. If the semi-coke in the proposed device was obtained not due to the combustion of additional fuel in the form of finely divided semi-coke supplied through the annular gap 48 to the muffle of the bypass pipe 16, but due to the burning of the dust supplied to the coking, when additional air is supplied, the percentage of carbon in the semi-coke would be less, and could not provide the optimal ratio of components when preparing the charge in a twin roll mixer 1. In the proposed device, the coking of dust in the lower section 15 of the dust concentrator 6 is performed and the account of the primary air in which part of the dust burns out, providing coking of the remaining part of the dust, as well as by heating the dust through the hot wall of the bypass pipe muffle 16. This increases the percentage of carbon in the charge.

Installation of additional swirls together with inlet nozzles in the lower section of the dust concentrator, between the lower end blade vortex swirl and the transverse partition, with the blades tilted in the same direction as the blades of the lower end reversible swirl swirl, with a step between swirls equal to the cross-sectional height of the lower dust flares input tangential nozzles, allows you to ensure, when dust is supplied simultaneously to the lower and upper input nozzles of the lower section of the dust concentrator, dust is lifted into the dust concentrator from the bottom to the top, due to cutting off the upper part of the torches from the upper inlet pipes with the opposite ends of the blades of the upper swirls, which prevents the fuel from falling down, and, therefore, the depth of semi-coking increases.

Perforation of the bypass pipe with openings located between the swirlers and near the transverse baffle allows the gas ballast to be continuously discharged into the bypass pipe with its subsequent afterburning in it, thereby separating the resulting semi-coke from the gas ballast, which increases the productivity and temperature of semi-coking, since instead of the removed gas , an additional amount of high concentration dust with primary air may be introduced into the space between the swirlers.

Perforation of the bypass pipe with holes located at the transverse partition allows you to get rid of fly ash in the upper section of the dust concentrator, through the hole above the transverse partition, and from the gas ballast in the upper part of the lower section of the dust concentrator, through the hole under the transverse partition, which increases the dust concentration in the branch pipe concentrated mixture located under the septum.

Perforating the bypass pipe in a dust collector half that is free of inlet nozzles eliminates large uncropped dust from entering these holes, since in a dust collector half that is free of inlet nozzles, the dust will be squeezed to the wall of the dust concentrator by centrifugal forces and will not enter the openings.

Placing the outlet section of the bypass pipe inside the waste pipe of the dust concentrator, with the formation of an annular gap between them, and connecting it to the lime hopper, allows you to replenish the lime hopper with the ash residue of thermal processing of oxidized coal, which contains up to half the calcium oxide [1], which reduces the cost of the process by eliminating the use of calcium carbonate.

Placing one of the branch pipes of the concentrated mixture under the transverse partition of the dust concentrator allows you to select semi-coke when transporting dust from bottom to top in the dust concentrator, from the upper part of the lower section of the dust concentrator, which increases the productivity of the installation.

Thus, a solution to the problem is achieved. Those. the proposed device allows to increase productivity by installing additional swirls and inlet pipes, to increase the temperature of semi-coking by feeding the semi-coke into the bypass pipe and the depth of semi-coking by raising dust from the bottom up to the bottom section 15 of the dust concentrator, while ensuring the optimal stoichiometric ratio of the charge components for carbide production calcium.

Claims (1)

A device for producing raw materials for the production of calcium carbide, containing a two-chamber mixer connected to the semi-coke and lime hoppers with batchers, and a semi-coke cooling system with semi-coking gases, as well as a vertical cylindrical dust concentrator for the thermal processing of oxidized brown coal, connected to the indicated semi-coke bunker, having axial and tangential upper and lower inlet nozzles, discharge pipe and tangential branch pipes for concentrated mixture discharge, separated by transverse a rod to the upper and lower sections, communicating with a bypass pipe, at the ends of which there are upper and lower reversible blade swirls, between which are located the upper and lower inlet nozzles connected by a dust collector with a gate through a dust pipe with a dust hopper, and a fuel oil nozzle is placed in the axial inlet pipe and an air nozzle, while the branch pipes of the concentrated mixture of the dust concentrator are connected to the semi-coke bunker, and additional swirls, characterized in that the additional Numerous swirls are installed together with the inlet nozzles in the lower section of the dust concentrator, between the lower end blade vortex swirl and the transverse baffle, with the blades tilted in the same direction as the blades of the lower end swirl reverser, with a pitch between swirls equal to the cross-sectional height of the lower dust plume inlet tangential nozzles, and the overflow pipe is perforated with holes located between the swirlers, and at the transverse partition, made in half of the housing trattoria, free from inlets, and the outlet portion of the overflow tube is placed inside the waste pipe pylekontsentratora to form an annular gap therebetween, and is connected to the lime hopper, wherein one of the nozzles discharge the concentrated mixture is placed under a transverse partition.