ES2261800T3 - PARALLEL FLOW CUBE REACTOR. - Google Patents

Abstract

A direct flow shaft reactor comprises a vertical shaft body (10) having a drying zone (14) for drying and heating the waste material, a degasifying zone (16) connected to the drying zone for degasifying the waste material, and a gasifying zone (18) for gasifying the waste material; a receiving body (20) connected to the shaft body for receiving molten waste material; and a gas removal unit (26) connected to the shaft body and/or the receiving body for removing the gases produced. Several gas feeding units (46) are provided in the transport direction of the waste material in the gasifying zone for feeding a gas into the degasifying zone. Preferred Features: The gas feeding units are uniformly distributed, preferably in a horizontal plane. Additional gas feeding units are provided in the drying zone and/or in the gasifying zone. The shaft body is cylindrical.

Description

Tank reactor with parallel flow.

The present invention relates to a reactor of parallel flow tank for casting and gasification of food substances of different types and consistencies, such as sticks, furniture and household appliances out of use, household waste, substitute fuels, pelletized animal powders or flours, plastics, industrial and business waste substances, free of polluting substances and / or loaded with substances pollutants

In gas reactors a gas can be produced synthetic, which is appropriate for energy production electrical, as well as heat, and / or find employment as a basis for synthesis processes As solid product generates a slag not leachable and a materially transformable metal phase or a non-elutable liquid phase, which is available for a broader transformation.

Document DE 43 17 145 C1 describes a procedure and a mechanism for degassing of waste materials on the basis of a flow tank oven Reverse heated with coke. In this respect it is fully extracted the generated gas laden with dust, and burns in the area of overheating and casting found under oxygen at high temperatures The counter-current guidance of the gas through of the discharge that moves down and the aspiration between the aspiration of circulating gas and gas supply in circulation give multiple practical problems. The consequence is short circuits in the tank and heat transfer insufficient in the upper cuba region, so a gas loaded with polluting substances with dust parts and tar. This is why expensive conditioning and gas purification. In addition, there is a danger that the continuous operation by dust and tar deposits. Other Permanent danger to stable operation is the guidance of pyrolysis and degassing gas with proportions of dust and tar in the ducts. The complete displacement or in some duct points with dust and tar deposits have as a result an irregular guidance of the gas in circulation, and with This is an irregular guidance of the process in the Cuba oven.

Document DE 196 40 497 C2 describes a gas dome oven in circulation heating with coke for the material and / or energy use of waste materials. It consists of a vertical oven vat with extraction openings of gas in circulation, large volume, placed horizontally below the loading mouth, which are joined by channels and nozzles with the zone of overheating and casting, above of which a plane of aspiration of gas in excess of large volume Remove the generated gas from the process. In addition, it is narrowed transversely the cuvette part of the oven between the opening of Extraction of excess gas and the opening of circulating gas. The Heat transfer is done, as also in the DE document 43 17 145 C1, for the process gases that rise upwards in the principle of countercurrent, towards the feeding material. The multiple conduction against gas flow, through the discharge that moves down, does not make possible the treatment of a broad spectrum in the feedstock, despite a modification by transverse narrowing in the tank and expansion transverse in the gas outlet.

Continuing, in document DE 198 16864 A1, describes a gas dome furnace in circulation, in which it is arranged an excess gas aspiration below the zone of overheating and casting. That is why there is a counter current gasification and heat transfer in the Cuba's upper furnace region, where the gas is aspirated by large volume openings and conducts through channels / nozzles to the zone of overheating and casting. In gasification a subsequent countercurrent gas is reduced at high temperatures and long chain hydrocarbons are cracked. Through this provision reduces the negative influence of flows in short circuit.

The spatial proximity of endothermic processes with respect to the hearth zone and the extraction of excess gas extracts the necessary heat to the melt to ensure under all the operating conditions the necessary liquid discharge of melt

Document DE 100 07 115 A1 describes a reactor for gasification and / or smelting of materials feeding with a supply zone, a gasification zone and degassing, as well as an overheating zone and foundry. The gasification and degassing zone has a transversal expansion as a gas supply space in which flows at least one combustion chamber with at least one burner, through which flue gases are supplied Hot from a pouring cone. In addition, means of great energy through upper and lower injection means in the overheating and smelting zone region, as well as above the melt using oxygen lances and / or nozzles In these mechanisms the surface of reactor increased in the region of the transverse enlargement of the pyrolysis, because heat losses appear. In addition, the gases hot introduced in the discharge in parallel flow form preferred flow channels which results in a non-homogeneous reaction on the reactor section.

Generally, it can be based on the basis that, for food substances with high flash point with poor heat conduction, and for materials with high humidity, the heat supplied in the gasification and degassing zone does not lead to sufficient heating and pyrolysis or to degassing of substances. The gasification processes and degassing move to the region of the area of overheating and smelting, and thus reduce reaction time for the destruction of all oils and tars formed in Long chain hydrocarbon form. To avoid this you should supplied so much heat that they would be partially produced in the bulk product areas so hot that they could damage the wall of the reactor, and thereby would significantly reduce the time of operation of a tank reactor.

All tank reactors described previously they can only be used for a limited range of feeding substances In addition, for the gasification of feed substances must be supplied an amount considerable energy. This is done especially by combustible materials introduced together with the bulk product or the feeding material in the body of Cuba, such as coke or Similar. In addition, for known Cuba reactors there is problem, regardless of whether they work with the flow principle parallel or countercurrent, that the removed gas is heavily loaded with particles, and with it must be filtered by example before a treatment.

The object of the invention is to make a parallel flow tank reactor with which, also with the use of different feed substances, gases can be produced useful, especially combustible useful gases with a load limited particles, whose production reduces the danger of a damage to the parallel flow tank reactor.

The solution of the objective is carried out according to the invention according to the characteristics of claim 1.

The parallel flow tank reactor according to the invention for the casting and gasification of material Feeding features a vertical bowl body. Inside the body of Cuba dries, heats and gasifies the feeding material. With this, the vertically arranged Cuba body presents successively in the direction of transport a drying zone for drying and heating of the feed material, an area of adjacent degassing here for material degassing of feeding and a gasification zone for the gasification of the feeding material. The body of Cuba is followed by a body of Reception that serves to receive food materials melted Within this body the foundry zone is formed of the reactor. The Cuba body and / or the receiving body are connected with a gas evacuation device for evacuation of useful gases produced inside the reactor. The device of evacuation is specially arranged in the region between the Cuba body and reception body, and made as a conduit. In addition, the vertically directed Cuba body has a supply device, through which the tank reactor feed material. In the zone of degassing are successively linked in the direction of transport of the feeding material, that is, in a body of vertical tank in vertical direction, with the body of Cuba a plurality of gas supply units in the area of degassing Through the gas supply units, which They are usually nozzles or similar, gas is supplied in the area degassing, by means of which it is seconded or accelerates the degassing of the feeding material.

The lower or narrower cylindrical region of the gasification region, if necessary, enter the area of foundry. On this part, at least partially, the discharge column, at the same time high temperatures reign there. For the assurance of mechanical rigidity and protection against high temperatures, according to the invention, a cooling by indirect water cooling on the wall of reactor vessel. As it is disadvantageous, for temperatures very high and the size of the region to be cooled, an embodiment in double wall of the reactor tank wall, because of the overheating that appears and destruction for it caused, this cylindrical or narrow region is made according to the invention as a coil. A coil shaped spiral through which a cooling medium is circulated, is especially suitable for cooling in This region. In particular, selective cooling is possible. The danger of vapor formation inside the coil is very reduced due to liquid circulation. The coil is preferably joined in a plurality of regions with inputs and separate outlets, so that the heated coolant too strong can be evacuated immediately from the coil.

Therefore, evaporation of the liquid is avoided refrigerant by vapor formation and the diminishing effect refrigerant attached to it. Between the rings or the spiral parts individual coil can be additionally provided burners or nozzles, so that the process control can be controlled very precisely also in this region. With that, the temperature in this temperature can be adjusted exactly region, regulation is preferably carried out separately and with this independent of the regulation of the burners and nozzles remaining.

Because of the successive arrangement of a plurality of gas supply units in the direction of transport can be better used the degassing zone, of so that it is also possible for food substances different degassing of these substances. As per the Gas supply in the degassing zone is introduced into special energy and with it heat in the degassing zone, in the degassing zone on the section can ensure a more regular heating of the feeding material. As per the invention are arranged behind each other a plurality of gas supply units in the transport direction, preferably continuous heating of the feeding material in the transport direction. Thus, it is possible that also difficult feeding materials of degassing is degassed in the degassing zone. How degassing is therefore carried out mainly in the degassing zone of the parallel flow tank reactor according to the invention prevents or reduces degassing of the material of feed in the smelting or gasification zone. Therefore, the Cuba reactor performance can be substantially raised. By means of the tank reactor according to the invention, a high degree of degassing in the degassing zone, of so that useful fuel gases can be produced that only They have a very small particle load.

To make heating as much as possible regulate possible feeding material in the area of degassing, gas supply units preferably They are arranged essentially distributed regularly. The gas supply units thus have a distance essentially equal to one another. In this regard preferably the individual gas supply units or a plurality of supply devices assembled respectively in a group or supply unit they are attached to a device control. With the help of the control device it is possible to regulate or control the gas supply units separately individual and / or supply units. This can be done, for example, by regulating the amount of gas delivered by the individual gas supply units of the oxygen content of the gas supplied and / or the temperature of the gas supplied. In addition, the mixture of gas.

The invention is explained below by a preferred embodiment in reference to the drawing attached.

The figure shows a schematic side view of a parallel flow tank reactor.

The parallel flow tank reactor has a tank body 10. The tank body 10, in the presented embodiment, can be subdivided into a transfer channel arrangement 12, a drying zone 14 adjacent to the channel arrangement of transfer 12, a degassing zone 16 adjacent to the drying zone 14, as well as a gasification zone 18 adjacent here. The gasification zone 18 of the tank body 10 is followed by a receiving body 20, which serves to receive the molten feed material. In the upper region of the receiving body 20, the casting zone 23 is formed. In the boundary region between the gasification zone 18 and the receiving body 20 the section of the receiving body is extended, so that a space of gas storage 24 made in the form of a ring, which surrounds the lower part of the gasification zone 18. The gas storage space 24 is connected to a gas suction device 26, made in the embodiment shown as a conduit -
to.

The feeding material is introduced into the tank body 10 through a supply opening 28 through the transfer channel arrangement 12. Material supply Power is done through the channel layout of transfer to avoid introducing a lot of ambient air through which the gasification and smelting process may be affected uncontrollably. Therefore, the provision of transfer channel features two channel devices transfer or transfer channel doors 30, 32, between that the transfer channel chamber 34 is made, being already the transfer channel chamber 34 a part of the body of Cuba 10.

Then, the feeding material reaches through the provision of transfer channel 12 to the zone of drying 14. In drying zone 14 and subsequent zones 16, 18 Cuba body 10 is almost completely filled with material power during operation. In the drying zone 14 neither does it form any or at most a small spout cone near the door of transfer channel 32. Thus, the Cuba body 10, at least in the region of the area of degassing 16, is performed cylindrically or widened free of jumps in the direction of transport. With it, the wall Cuba interior of Cuba body 10 is flat at least in the area degassing 16, and does not have any steps or the like.

In the embodiment shown, it is provided in the region of the drying area of the body of Cuba 10 a gas supply unit 36. The gas supply unit 36 has an annular conduit 38 that surrounds the tank body 10, which is connected with a plurality of nozzles 40 distributed regularly on the perimeter. Through the supply unit Gas supply material 36 is supplied in the region of the drying zone 14, preferably hot air, which given the case may be enriched with oxygen, for drying the feeding material.

In the degassing zone 16 adjacent to the drying zone 14 is provided a plurality of devices of gas supply 46, which are especially nozzles. In the zone of degassing 16 are arranged regularly distributed gas supply devices 46. In particular they are arranged successively in the direction of transport of the material of feeding, that is, in the figure from the top down, a plurality of gas supply devices or nozzles 46. It preferably it is at least three nozzles 46 arranged successively. In the embodiment shown, they are joined several nozzles 46 forming a supply unit 42. By thereby, an annular conduit 44 is provided, through which the nozzles 46 can be supplied together with gas. With it, the duct annular 44 is preferably connected to a plurality of nozzles 46 regularly distributed around the perimeter. Each annular duct 44 It has in particular at least three nozzles. Annular ducts 44, which are arranged each time in a horizontal plane, form together with the nozzles or gas supply devices 46 42 independent supply units. Within the zone of degassing 16 several supply units are arranged 42, four in the embodiment shown. According to invention is especially preferable to provide at least two units of supply. The individual supply units 42 are arranged displaced or rotated relative to each other, so that in the direction of transport of the feeding material are arranged nozzles 46 arranged successively not on or one after other but displaced or next to each other. Supply units  individual are preferably arranged in front of the unit of supply arranged above rotated each time at the same angle. In this regard, the size of the angle of rotation is preferably dependent on the number of nozzles 46 provided per unit of supply 42, so that a deal is essentially made regulate the nozzles 46 in the degassing zone 16. Through of the gas supply devices 46 can be supplied to the feeding material high energy gases, oxygen, air or other gases suitable for the control of the gasification process and foundry.

Other nozzles 48 are provided in the area of gasification 18. Through the nozzles 48 can be supplied with new high energy gas or other gases or substances that control the gasification and fusion process. They can also be provided instead of nozzles 48 also burners, which supply in the gasification zone 18 directly heat the material of feeding. The final region of the body of Cuba 10 with symmetry of rotation with respect to the longitudinal axis 50 is performed conically slightly narrowed, so that the feeding material is retains a little in the region of the gasification zone 18.

In addition, on a side wall 52 of the body of reception 20 are arranged a plurality of nozzles 54 distributed around the perimeter. The nozzles 54 are used for introduction of high energy gases or similar substances. Through the nozzles it is guaranteed that the melt 22 stay liquid They can also be provided instead of nozzles 54 also burners.

A side wall 56 of the channel arrangement Transfer 12 is preferably made of double wall. Therefore, it can be heated, and with it a material drying feed into the transfer channel chamber 34 while a hot medium is driven by the double wall side wall 68. In this case it is preferably air or other gas. In special it is possible to provide the gas supply unit 36 in place in the region of the drying zone 14 in the region of the transfer channel arrangement 12.

The transfer channel arrangement 12 It has the objective of the homogeneous and continuous supply of material, and the tight seal against the environment.

The ideal material input requires preferably a homogeneous mixture, especially for the Dosage of additives such as coke and lime. The entry occurs according to the central invention on the axis of the reactor. The volume of the transfer channel chamber 34 is used if possible completely, and falls into the reactor vessel if possible in equal diameters The reactor should be kept full if possible. In continuous operation. Therefore, a level control it is preferably placed directly under the door of the transfer channel 32. Filling is done at a rate high. By these measures the entrance is diminished at the same time of incorrect air, and the maintenance of pressure in the total system

According to the invention, the regions, arrangement of transfer channel 12, drying zone 14 and zone of degassing 16 even in the gasification zone 18 are preferably made cylindrical or extending slightly conical down. The transition between the zones is done without discontinuous or step-shaped section extensions, is that is, the transition is from the same section, and without formation of empty spaces, steps or ridges, free of stacked beds.

Also, the drying zone 14 may be made of double wall especially for constructive forms bigger. This makes possible the indirect heating of the product column inside or securing a regular temperature on the wall, and a decrease in appearance of condensation on the inner face. Also as a medium Heat transmitter is preferably used hot air.

In heating the output product has place the evaporation of water in the drying zone 14. The temperature in the product increases in this only little over the 100 ° C During the course, with increasing temperature they are released absorbed gases such as nitrogen and carbon dioxide, which are not They are generated by dissociation reactions. At the latest here You can talk about degassing. Above 250 to 300 ° C then the generation of gases and vapors begins, in which case deals with low molecular weight distilled and first compounds dissociation products. Another increase in temperature causes development of reactions that lead to the formation of methane and hydrogen.

Also, the degassing zone 16 can be formed of double wall following the drying zone 14.

In the lower third of the drying zone and degassing 14, 16 is a region in which the inside temperature of the reactor is higher than the temperature of the hot air. Here the double wall embodiment can be replaced by a refractory silicate coating. An embodiment of the drying and degassing zone 14, 16 total is advantageous with a pressed mass, also in a double wall embodiment. The Small heat transfer and resistance to change reduced temperature are opposed to the small wear of the steel structure shirt.

For the next heating of the column of discharged at approximately 700 ° C is done, next to the transformation of combustible material under the influence of heat, the heterogeneous reaction between the combustible material and the oxygen from the air that has not yet reacted.

The gasification zone 18 is the zone of main reaction inside the tank reactor. Here it is done to temperatures from 1,200 to 1,400ºC the energy transformation and solid substances material. Solid fuel material gases and solid products originate from coke to ash. For the uniform and complete reaction is decisive that a spill homogeneously circulate evenly through degassing gas already generated and the means of gasification to be introduced here. The area of gasification 18 must present for these reasons a height enough. This is achieved in this regard thanks to the area of gasification 18 is realized as a cylindrical straight region with transition in a conical reduction of the section, or immediately As increasing decline. As the grain of material is reduced by the material transformations and related forces that destroy, thereby, increase the empty spaces within the spill column For the reduction of the section of Cuba in this region the rate of descent of the column can be homogenized of material. Flow channels are destroyed and formation is avoided of larger empty spaces in the landfill.

Also, following the area of degassing 16 located above, the region of Gasification is coated with a mass of silicate.

The gas circulates in parallel flow with the material supply the high temperature gasification zone 18. Long chain hydrocarbons, generated from the actions of degassing and thermolysis have been dissociated here thermally, and at the same time were involved in the processes of gasification elapsed Value fuel gas is generated medium calorific with the main components monoxide of carbon, carbon dioxide, hydrogen and water vapor without condensable hydrocarbon components. Many of the reactions Chemicals run simultaneously are endothermic. With that, the temperature of the gas is reduced as that of the discharge.

In the lower or decreased cylindrical region of the gasification region 18, which goes into the case in the casting zone 23, the coil 60 is arranged according to the invention. It is preferably provided with inputs and outputs separate not shown in the figure. In addition, between the rings or individual spiral parts of the coil can be provided with nozzles 48 or additional 54 burners. Below the refrigerated region by gas from the gasification region 18 the gas experiences a deviation of approximately 180º and reaches space 24 free of stacked beds. By endothermic processes, described above, The gas has a temperature of approximately 1,000 ° C. After one some soothing and homogenization of the gas the gas is aspirated above outside the reactor.

The gas accumulation space 24 is already casting zone component 23, which is above essentially beyond the gasification zone 18 that is enters, and surrounds the gasification zone 18 at least partially. The cylindrical casting zone 23 is conically reduced towards below and ends with the floor plate, above which stores the phase separated by fusion.

Foundry zone 23 is provided in its whole with a pressed mass of several layers, or is endowed With a refractory lining. Reason for this are the high temperatures needed. Only in the space region of gas storage is not necessary eventually a coating refractory.

The solid completely degassed and coked, it is molten or sintered already in some points and descends from the gasification zone 18 then to the zone of foundry 23.

In the foundry zone 23 an integrated plane with a plurality of nozzles or oxygen injectors and / or 54 burners that work by oxidation, which are also distributed symmetrically on the axis.

For the gas supply with a concentration of high oxygen you get strong exothermic reactions with the gas and the gasification zone solid 18. They are produced temperatures those that are clearly above the point of melting of the material, usually approximately 1400 ° C at 1600 ° C. In the region of oxygen nozzles even occur hot temperature zones from 1800 to 2000 ° C. Under these conditions, adding slag formers and / or materials that reduce the melting point, melt apart Safe all inorganic harmful substances.

Melt-separated material is stored as melt in the reactor floor. The emptying of this mass Liquid melt is done as usual in a workshop foundry, through a piquera and a casting channel 72. It is possible a constructive form with antecrisol or siphon.

With a constructive form sufficiently large and corresponding timeout of the foundry mass the melt will be separated into a heavy metal phase and a scum floating on it. Here there is the possibility of being able to win over differently high drains a metal phase Usable and scum. In the slag product they are not contained organic substances and inorganic components are stably housed in a silicate matrix. The use is known as material for the construction of roads, dumps and ports, it is also possible to manufacture special molds and products like those that are common in the industry glass.

Claims (13)

1. Parallel flow tank reactor for the fusion and gasification of feed material, with a vertical bowl body (10) with a drying zone (14) for drying and heating of the feeding material, a degassing zone ( 16) adjacent to the drying zone (14) for the degassing of the feed material and a gasification zone (18) for the gasification of the feeding material, the feeding material being transported from the drying zone (14) through from the degassing zone (16) to the gasification zone (18), a receiving body (20) adjacent to the tank body (10) for receiving the molten feed material (22), and an evacuation device for gas (26) connected with the tank body (10) and / or the receiving body (20) for the evacuation of the generated gas, being provided successively in the direction of transport of the feed material in the degassing zone (16) a pl urality of gas supply units (42) connected with the tank body (10) for the supply of gas in the degassing zone (16), characterized in that in the tank wall of the reactor in the region of the transition between the gasification zone (18) and the smelting zone (23) a coil (60) is provided for temperature control. 2. Parallel flow tank reactor according to claim 1, characterized in that the coil (60) has a spiral shape. 3. Parallel flow tank reactor according to claim 1 or 2, characterized in that a region that narrows in the direction of transport of the feed material is made by the coil (60), especially the region narrows conically. 4. Parallel flow tank reactor according to one of claims 1-3, characterized in that the coil (60) is connected in a plurality of regions with the separate inputs and outputs. 5. Parallel flow tank reactor according to one of claims 1-4, characterized in that the gas supply devices (46) are arranged essentially distributed regularly. 6. Parallel flow tank reactor according to one of claims 1-5, characterized in that at least three gas supply devices are successively provided in the transport direction. 7. Parallel flow tank reactor according to one of claims 1-6, characterized in that a plurality of gas supply devices (46) are arranged in a horizontal plane. 8. Parallel flow tank reactor according to one of claims 1-7, characterized in that the gas supply devices (46) arranged in a plane are connected with an annular conduit (44) to form a supply unit (42) . 9. Parallel flow tank reactor according to claim 8, characterized in that the gas supply devices (46) of the supply units (42) arranged successively in the transport direction are arranged displaced relative to each other. 10. Parallel flow tank reactor according to one of the claims 1-4, characterized in that nozzles (48) or burners (54) are especially provided between the individual spiral rings or parts (60) which are especially separately adjustable. 11. Parallel flow tank reactor according to one of claims 1-10, characterized in that the gas supply devices (46) and / or the supply units (42) are connected to a control device. 12. Parallel flow tank reactor according to one of claims 1-11, characterized in that additional gas supply devices (46, 48) are provided in the drying zone (14) and / or in the gasification zone (18). . 13. Parallel flow tank reactor according to one of claims 1-12, characterized in that the tank body (10), at least in the region of the degassing zone (16), is made cylindrical or extends without jumps in The transport address.