DE4217110A1 - Fluidised bed reactor with inclined shaft - Google Patents

Fluidised bed reactor with inclined shaft

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Publication number
DE4217110A1
DE4217110A1 DE19924217110 DE4217110A DE4217110A1 DE 4217110 A1 DE4217110 A1 DE 4217110A1 DE 19924217110 DE19924217110 DE 19924217110 DE 4217110 A DE4217110 A DE 4217110A DE 4217110 A1 DE4217110 A1 DE 4217110A1
Authority
DE
Germany
Prior art keywords
nozzle
fluidized bed
bed reactor
characterized
reactor according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
DE19924217110
Other languages
German (de)
Inventor
Heinrich Wagener
Reinhold Kirchhoff
Hans-Joachim Jagnow
Helmut Sadowski
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bergwerksverband GmbH
Original Assignee
Bergwerksverband GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Bergwerksverband GmbH filed Critical Bergwerksverband GmbH
Priority to DE19924217110 priority Critical patent/DE4217110A1/en
Publication of DE4217110A1 publication Critical patent/DE4217110A1/en
Application status is Ceased legal-status Critical

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Classifications

    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23CMETHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00Fluidised bed combustion apparatus
    • F23C10/18Details; Accessories
    • F23C10/20Inlets for fluidisation air, e.g. grids; Bottoms
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818Feeding of the fluidising gas
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/386Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only internally, i.e. the particles rotate within the vessel
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/44Fluidisation grids

Abstract

A fluidised bed reactor consisting of a reactor vessel and an oblique shaft fitted beneath it. Fluidisation gas apertures are integrated into the oblique shaft wall in several superimposed and mutually staggered nozzle planes and can be fitted with nozzle inserts, a fluidisation gas inlet is fitted behind the oblique shaft wall to which several horizontally superimposed blast box sections are allocated which can be operated by fluidisation gas pressures decreasing from bottom to top and a fluidised substance extractor is connected at the lowest part of the shaft. Into each fluidisation gas aperture in each nozzle plane (I, II, III, IV) is inserted a row of nozzles (5, 5a, 5b, 5c, 5d) inclined downwards at an angle of inclination ( alpha 1), each row of nozzles (5, 5a, 5b, 5c, 5d) consists of several adjacent individual nozzles (4, 4a, 4b, 4c, 4d) with a rectangular cross-section which widens from the inlet (71) to the outlet (72) of the nozzle, and the individual nozzles (4, 4a, 4b, 4c, 4d) are interconnected via a pressure equalising channel (11), and to each nozzle plane (I, II, III, IV) is allocated its own blast box section (6, 6a, 6b, 6c, 6d) of the fluidising gas intake.

Description

The invention relates to a fluidized bed reactor consisting from a reactor vessel and one below it Slant shaft, wherein in the oblique shaft wall in several Dü Senebenen one above the other and offset to each other Wirbelgasöff integrated and can be equipped with nozzle inserts, provided behind the inclined shaft wall a fluidizing gas supply and in the shaft deepest a Wirbelgutabzug is connected.

Fluidized bed reactors are fluidized with medium such as gas or Steam applied and z. For combustion, Gasification, drying, mixing, agglomeration application find.

Fluidized bed reactors with conventional nozzle plates, such as B. from DE-OS 32 23 182 is known from a number arranged in grid shape, usually the same height cans stick out of pipe socket, which is perpendicular to the underneath in a horizontal plane arranged side by side wind boxes are welded on top and attached with a distance mushroom-shaped or smooth cover lid are covered. The Fluidizing gas occurs in a horizontal plane. A ge Targeted coarse vortex discharge is in this horizontal design difficult.  

Compared to fluidized bed reactors with conventional nozzle plates allows the generic fluidized bed reactor with oblique bay a better coarse Wirbelgutabzug and in the Inclined shaft wall arranged offset, with nozzle inserts Equipped vortex gas openings and the lateral fluidizing gas supply facilitate the fluidization of the fluidized material and avoid caking. Disadvantages of this reactor are layout

  • - the difficult restarting and blowing of the individual nozzles that are less good for training rollers currents are suitable,
  • - the inadequate balance of pressure and speed of Fluidisiermediums because of ver the same small cross section of the fluidizing gas supply and because of the supply only through a gap and
  • - the combustion behavior causing the emissions in the Burning zones due to insufficient secondary air supply these areas.

The invention is based on the object, the aforementioned Disadvantages of an improved design and arrangement in particular the fluidizing gas feed and the vortex gas nozzles ei nes generic fluidized bed reactor to avoid.

This task is characterized by the characterizing features of Patent claim 1 solved. Advantageous developments are in the dependent claims 2 to 18 laid down.  

With the fluidized bed reactor according to the invention can be in particular realize the following advantages:

  • - In the case of a shutdown, there is no good overflow into the wind box sections of the fluidizing gas supply, as the Bulk material inclination within the single nozzle opening ends.
  • - When restarting is a problem-free blowing the Single nozzle opening on the smooth sloping nozzle running board possible.
  • - About the bundled in rows of nozzles individual nozzles is a good cross-mixing (dispersion) of the fluidized bed he be enough and the formation of roller flows of reached the nozzle rows.
  • - By partial filling of the inclined shaft with vortex bed material is an optimal part-load driving style feasible, because it will be only those with layer material covered nozzle rows of the lower nozzle levels with Whirling gas applied, while the rows of nozzles -oberen Nozzle levels by switching off the valves out of service ge can be taken.
  • - In addition, there is another alternative part-load driving wise through a graduated mode of operation, even if the entire reaction space with fluidized bed material is filled by only the nozzle rows of the upper nozzle levels are operated. The lower Bettbe rich is not fluidized and merely serves as cold ash-room. Especially in narrow reaction spaces can in this way only the upper bed fluidized and thus activated. In wide Reaction spaces, d. H. at larger distances between the nozzle-equipped shaft walls and switched off Dü Rowing in the lower nozzle levels only occurs in the  Area of the two walls of fluidized zones. at This driving style is the fuel or the product to be dosed accordingly close to the wall.
  • - Due to the interchangeability of as a component part made nozzle rows can the shaft walls of the Reaction space consist of both heat-resistant steel as well as be covered with ceramic insulating.
  • - Via the pressure equalization channel is between the single nozzles pressure equalization of the fluidizing gas caused, which guarantees that, despite possibly occurring Resistors in the nozzle exit always the desired vortex amount of gas can flow into the fluidized bed.
  • - By ge until the inner wall of the reactor vessel led height-graded arrangement of the nozzle rows with several The individual nozzles in nozzle levels are for each under expiring combustion sufficient seconds provided with compressed air, so that the harmful emissions can be reliably reduced in the entire fluidized bed NEN.
  • - By a down and at the same time laterally inclined An Order of the individual nozzles of the nozzle rows can be an additional Licher angular momentum causes parallel to the container inner wall and thus an even better mixing in Brennherdbe be achieved rich.

Advantageous embodiments of the vortex according to the invention layer reactor and its mode of action and other benefits will be explained by way of example with reference to the drawing. Show it:  

Fig. 1 is a schematic partially sectional view of a fluidized bed reactor with inclined chute,

Fig. 2 shows the object of Fig. 1 in a modified embodiment,

Fig. 3, 3a and 3b, details of a nozzle row of the object of Fig. 1,

Fig. 4 u. 4a details of a nozzle row of the article of Fig. 2,

Fig. 5 shows details of the inner wall of the object of Fig. 1 with a round cross-section inclined shaft,

Fig. 6, 6a and 6b another nozzle row assembly of the object of Fig. 5,

Fig. 7 is a cross sectional view of a nozzle row, together with schematic diagram of the Fluidisierbereiches,

Fig. 7a is a plan view of the object of FIG. 7,

Fig. 8 is a cross sectional view of a nozzle row of the object of Fig. 1,

Fig. 8 is a view of the object of Fig. 8,

Fig. 9 is a cross sectional view of a nozzle row of the object of Fig. 2,

Fig. 9a shows a view of the object of Fig. 9 and

Fig. 10 is a schematic diagram of a transparent Ver search model.

Fig. 1 and Fig. 2 show examples of the execution of fluidized bed reactors 1 , 1 a, consisting of reactor vessels 75 , 75 a with vertical container walls 22 a and below angeord Neten inclined shafts 2 , 2 a, the latter tapering downwards obliquely Have walls 22 . At the lowest point is a vent 8 , which serves to remove coarse ash and debris during operation, and to drain all other fluidized bed material after completion of an operating cycle.

In the obliquely disposed shaft walls 22 and the vertically disposed container walls 22 a nozzle according to the invention are rows 5 of a plurality of individual nozzles 4, 4 a, 4 b, 4 c, 4 d (Fig. 3a and 4a) are integrated. Behind the sloping shaft walls 22 are windbox sections 6 , 6 a, 6 b, 6 c of a windbox 84 is arranged to supply the rows of nozzles 5 , 5 a, 5 b, 5 c with We belgas.

The constructive simplicity of the nozzle rows 5 , 5 a, 5 b, 5 c ge equips it, the fluidizing gas -. B. air - before the Windkastenab cut 6 , 6 a, 6 b, 6 c with a in the fluidizing gas line 53 a built-in burner 27 ( Figure 2) preheat for energetic reasons, without causing distortion damage to the individual nozzles 4 , 4 a, 4 b, 4 c, 4 d arise. The heightwise arranged in nozzle planes I, II, III, IV, V ( Fig. 6) staggered rows of nozzles 5 , 5 a, 5 b, 5 c, 5 d, to compensate for the upward decreasing pressure difference in the fluidized bed 7 , with be acted upon under different amounts of gas. For this purpose ( Fig. 1 left) the fluidizing gas supply via a valve register 28 or ( Fig. 2 left) on different sized partition wall openings 61 , 61 a, 61 b, 61 c in partitions 30 of the windbox sections 6 , 6 a, 6 b, 6 c controllable. In circular reactor chambers 31 , 31 a ( Figures 1 and 2 left), the upper larger process space cross sections in the inclined shafts 2 , 2 a are supplied with a correspondingly more fluidizing gas.

The reactor walls consist of a heat-resistant steel wall 23 ( FIG. 1) or a ceramic insulating wall 24 or a ceramic brick wall 24 ( FIG. 2). In both cases, it is possible to work with the same construction of the nozzle rows 5 , 5 a, 5 b, 5 c. As a result, a very economical construction is possible. Whether a steel wall 23 or a ceramic Iso lierwand 24 is used, decide the respective eco nomic or procedural criteria. In this case, the required process chamber temperature and the desired service life - especially in abrasive fluidized bed material - to be considered.

As shown in FIG. 1, formed in the near-wall areas of the fluidized bed 7 roller flows, as flow arrows 14 illustrate, whereby a good burnout in the rows of dunes 5 , 5 a, 5 b, 5 c adjacent, well-stirred combustion zones is reached ,

The fluidizing gas passes via a fluidizing gas conduit 53 ( FIG. 1) or 53 a ( FIG. 2) into the windbox sections 6 , 6 a, 6 b, 6 c, wherein in FIG. 1 fluidizing gas conduits 82 , 82 a, 82 b, 82 c with integrated valves 16 , 16 a, 16 b, 16 c, a regulation of the fluidizing gas supply in the windbox sections 6 , 6 a, 6 b, 6 c he let. In Fig. 2, a simpler alternative is provided in which over different sized partition wall openings 61 , 61 a, 61 b stepped amounts of fluidizing gas in the wind boxes 6 , 6 a, 6 b, 6 c reach.

The product or fuel supply to the fluidized bed via product or Brennstoffdosieröffnungen 54 , 54 a in the reactor vessel 75 , 75 a and / or directly in the fluidized bed 7 of the inclined shaft 2 , 2 a, where the mixing takes place with the fluidizing gas , Grobasche and foreign parts will be deducted as possible on the ash deduction 8 by a flat slide 55 is actuated.

The reactor vessel 75 , 75 a may be formed as a round container 57 , 57 a or as a rectangular container 58 , 58 a.

Details "A" ( Figure 1) and "B" ( Figure 2) are shown in Figures 3, 3a, 3b and 7, 7a ("A") and in Figures 4, 4a ("B"). ) and described in more detail below:

Fig. 3, 3a, 3b and Fig. 4, 4a show in cross section the structural design of the nozzle row 5 in the shaft wall 22 , wherein Fig. 3 relate to the installation in a heat-resistant steel wall 23 and Fig. 4 the installation in a ceramic Isoliermassewand 24 , For each nozzle row 5 ( FIG. 3), a nozzle seat 9 is recessed in the oblique shaft wall 22 (FIGS . 3b and 4a). The width corresponds to the respective number of individual nozzles 4 , 4 a, 4 b, 4 c, 4 d of the nozzle row 5 ( FIG. 3 b). The height is formed from the angle of inclination α1 between the intermediate wall 30 (in the windbox 6 ) and the nozzle outlet plate 13 ( FIGS. 3 and 4). The rectangular in the example nozzle inlet 71 is limited in height by the intermediate wall 30 and the nozzle outlet plate 13 . Laterally, the nozzle inlet 71 is determined by spacer plates 62 arranged on the right and left. The nozzle hole 10 widens in the direction of the nozzle exit 72 and is laterally bounded by the process space 26 extending to the Leitblechrippen 63 , 63 a. The baffle ribs 63 , 63 a are welded in the nozzle seat 9 and contribute together with a reinforcing rib 59 substantially to maintain the strength of the shaft wall 22 at. Between the spacer plates 62 and the baffle ribs 63 , a pressure equalization channel 11 between the individual nozzles 4 , 4 a, 4 b, 4 c seen before. The one row of nozzles 5 final outer side blechrippen 63 a are firmly connected to the spacer plates 62 .

If the shaft inner wall surface 22 is covered with ceramic insulating compound 24 ; is a Unterleg-metal skin 34 constructively arranged to the Iso lierwandstärke outward. The spacer plates 62 are here below the lining sheet metal 34th For static reasons - support the Isoliermassewand 24 - extends the intermediate wall 30 into the Isoliermassewand 24 into it. The height dimension of the nozzle outlet 72 results from the inclination angle α1 between Isoliermassewand 24 (lower edge) and inter mediate wall 30 (lower edge) and nozzle outlet plate 13 (top edge). The steel leading edges 35 of the Leitblechrippen 63 and 35 a of the nozzle outlet plate 13 have contact with the fluidized material. The cooling by the outflowing fluidizing gas, however, lowers the working temperature in this range and thus increases the service lives of these elements. A occurring after a long time wear or removal of the steel leading edges 35 , 35 a is manageable and does not affect the operation.

In FIGS. 5 and 6, 6 a, 6 b, examples of the division and equipping of inclined shaft wall inner surfaces 22 and vertical container inner wall surfaces 22 a with rows of nozzles 5 are listed.

Fig. 5 shows a round process chamber 26. The lower nozzle plane I (smallest diameter) is equipped with a large number of short lower nozzle rows 20 . These rows of nozzles 20 are located in the shaft deepest and are arranged around the center hole 12 for the Wirbelgutabzug around and guarantee the Fluidisa tion in the process chamber center. Simultaneously, the lower rows of nozzles cause 20 that just above the center hole 12 takes place a continuous fluidization which detects all active Wirbelgutmaterial to the end of an operating cycle, whereas the inactive rough parts are abklassiert 65 through the center hole 12 in the trigger. 8

The middle rows of nozzles 5 b, 5 c in the middle nozzle planes II, III and the upper nozzle rows 15 in the upper nozzle plane IV are each offset to the next lower nozzle rows arranged and in their length and thus Leistungsfä ability of each Fluidisiergasmenge required in jewei time Reactor cross-section adapted. The upward decreasing pressure loss corresponding to the respective fluidized bed height is taken into account in the fluidized gas supply, as mentioned above.

Fig. 6 shows the arrangement of the nozzle planes I, II, III, IV, V and the nozzle rows 5 in a rectangular in the upper part Re actorraum 38 and in the lower part pyramidal reactor chamber 87th A well-adapted division of the nozzle rows 5 and the Dü senebenen I to V over the entire cross section shows z. B. Fig. 6b. Otherwise, the same criteria apply as in the above-mentioned round process chambers 26 with respect to the respectively required fluidizing gas for the respective reactor cross-section. The classification of coarse material 65 via the center hole 12 is supported by inclined guide surfaces 64 laterally below the reactor space 87th

From FIGS. 7 and 7a, the formation of the fluid mechanics in the fluidized bed 7 emerges. The outlet of the fluidizing gas triggers over the upper tear-off edge 39 on the shaft inner wall surface 22 of an inwardly rotating, marked by flow arrows 40 roller. As a result, rising fluidized bed material 67 enters a fluidizing region 70 in the wall region and is directed from there to the shaft inner wall surface 22 . The downwardly rotating fluidized bed material 67 again captured by the fluidizing gas is then conveyed into the ascending fluidizing region 69 at the center of the shaft. This flow picture is repeated in all reactor cross-sectional areas with nozzle rows 5 . This causes a very intense horizontal and vertical mixing of the fluidized bed material 67 between the nozzle planes 1 to V with nozzle rows 5 (see also Fig. 1). In the central fluidized bed axis 42 , although the tendency of an upward movement of good by fluidization outweighs, between two rotating rollers, however, a horizontal and a descending movement is also partially present, so that an overall optimum turbulence of the fluidized material is achieved.

The movement processes of the running fluid mechanics, triggered by the rows of nozzles 5 shown here , contribute to the fact that the residence time of the fuel or the product compared to conventional fluidization with flat nozzle plates in the fluidized bed 7 is considerably longer and thus a better and more economical use z. B. a fuel is guaranteed.

About the pressure equalization channel 11 communicate the individual nozzles 4 , 4 a, 4 b, 4 c, 4 d each row of nozzles 5 with each other, so that the individual Wirbelgasfäden (flow arrows 68 ) enter with approximately the same energy contents in the fluidized bed 7 and unite to vigorous fluidizing gas streams ,

A simplified embodiment of lowered nozzle rows 5 is particularly advantageous for equipping larger numbers of fluidized bed reactors 1 , 1 a and allow an even more rational design of the same. Fig. 8 and 8a, and Fig. 9 and 9a show the structural design of such rows of nozzles 5 on the modular principle (Fig. 8 and 8a, in conjunction with a heat-resistant steel wall 23 and Fig. 9 and 9a, in conjunction with a ceramic Isoliermassewand 24) These nozzle rows 5 can be completely prefabricated as a welded prefabricated part or as a cast finished part. In the latter can come before geous die casting or in particular the investment casting.

Modular principle states that welded or cast finished parts 73 , 73 a are manufactured for a certain base length of a row of nozzles 5 , which are welded side by side depending on the required performance to nozzle groups. In tight spaces, smaller base lengths can also be created and installed by cutting. It is also possible, at the base lengths of the nozzle inputs 71 bring to zoom by welding beads or to increase the nozzle inputs 71 by grinding in order to reduce or increase the Wirbelgasgeschwin speed.

The construction of a row of nozzles 5 serving as structural parts welding or cast finished parts 73 , 73 a corresponds to a basic principle, Figs. 3 and 4 explain. The welded or cast finished parts 73 , 73 a consist of Leitblechrippen 63 and 63 a as side boundaries, Düsenauslaufblechen 13 and Düsenabdeck plates 13 a, which can be welded to the steel wall 23 with the nozzle outlet 72 and 34 in the lining sheet metal.

Another advantage of the applied modular principle is that the installation point in the inclined shaft inner wall surface 22 and the container inner wall surface 23 a can be arbitrarily selected and this does not have to be done below the respective inter mediate wall 30 in the wind box 6 . This can be made even more optimal division of the nozzle rows 5 on the inner wall surface 22 and container inner wall surface 23 a.

Furthermore, it is very advantageous that the rows of nozzles 5 can be welded into the steel wall 23 or into the underlay sheet metal 34 in any inclined position. Especially with fine-grained, flowing fluidized state horizontally flowing material can prevent by appropriate inclination of the nozzle row 5 that finite granular, fluidized fluidized bed material (angle of repulsion ß1) can overflow in the windboxes 6 , which in coarse eddy layer material (angle of repose β2) not at standstill the case would be.

Furthermore, there is the possibility, with oblique 22 or vertical walls 22 a ( Fig. 6a) equipped reactor rooms retrofitted with rows of nozzles 5 and the required wind boxes 6 .

It is also possible to incorporate such rows of nozzles 5 in conventional nozzle floors with vertical nozzle bars (denoted in the drawing). Upwardly closed round, rectangular or triangular pipe socket can be provided shortly below the end cover with recesses, in which the nozzle rows 5 can be welded.

Finally, it should be noted that the structural design of the nozzle row 5 with a given nozzle hole height and a performance nozzle hole width as the sum of horizontally juxtaposed rows of nozzles 5 - ultimately regarded as an elongated rectangular nozzle slot - can not be replaced by a variety of round conical nozzle tubes. The latter would be very difficult to install and not justifiable from the production price and with regard to the specific output to be generated.

In Fig. 10, a transparent model 74 of a fluidized bed reactor 1 is shown. Its reactor vessel 75 and the oblique shaft 85 arranged underneath, which has a wall inclination γS of 60 °, are equipped with rows of nozzles 5 whose inclination γD is 20 °. A compressor 80 and an air collector 79 generate compressed air, which is metered via solenoid valves 78 a to f and hand valves 77 a to k transported in fluidizing gas lines 53 to wind boxes 6 and passes through the nozzle rows 5 as fluidizing gas in the fluidized bed 7 , the semolina or Fine sand is filled as fluidized bed material. With this test device Ver could be demonstrated that when open solenoid valves 78 a to f a full load operation is simulated, the manual valves 77 a to k from edge to whirl are adjustable. Part-load operation is simulated by the solenoid valves 78 a to d or c to f be closed by a time ge ge.

The test facility has the following technical data.

Air interpretation Whirling in free cross section Cross section: 0.45 m × 0.03 m | = 0.0135 m² Air requirement at 1 m / s = 0.0135 m³ / s = 13.5 l / s Air capacity of the compressor = 20-30 l / s selected nozzle inlet = 4 mm × 30 mm 10 nozzles total cross section = 0.004 m × 0.030 × 10 pcs. = 0.0012 m² nozzle inlet = 0.0135 m³ / s: 0.0012 m² = 11.25 m / s min for semolina or fine sand

The experiments have optically confirmed that the staggered arranged rows of nozzles in the inclined shaft of Reactor, the mechanical fluid behavior of the fluidized bed significantly improved over the conventional technique can be.

LIST OF REFERENCE NUMBERS

1 , 1 a fluidized bed reactor
2 , 2 a inclined shaft
4 , 4 a, 4 b, 4 c, 4 d individual nozzle
5 , 5 a, 5 b nozzle row
5 c, 5 d middle row of nozzles
6 , 6 a, 6 b, 6 c, 6 d Windkastenabschnitt
7 vortex shaft
8 ash deduction
9 nozzle seat
10 nozzle hole
11 pressure equalization channel
12 center hole
13 nozzle outlet plate
13 a nozzle cover plate
14 roller flow arrow
15 upper nozzle row
16 , 16 a, 16 b, 16 c valve
20 lower nozzle row
22 inclined shaft inner wall surface
22 a container inner wall surface
23 heat-resistant steel wall
24 ceramic insulating wall
26 process space
27 integrated burners
28 valve registers
30 partition wall
31 , 31 a circular reactor space
34 underlay metal skin
35 Steel leading edge baffle rib
35 a Steel leading edge Nozzle outlet sheet
38 , 38 a rectangular reactor space
39 upper tear-off edge
40 flow arrow
42 central fluidized bed ash
53 , 53 a fluid gas line
54 , 54 a product or fuel metering opening
55 flat slide
57 , 57 a Round container
58 , 58 rectangular containers
59 reinforcing rib
61 , 61 a, 61 b, 61 c partition wall opening
62 spacer plate
63 , 63 a baffle rib
64 guide surface
65 coarse material parts
67 fluid bed material
68 fluidizing flow arrow
69 fluidisation area (shaft center)
70 fluidisation area (wall area)
71 nozzle inlet
72 nozzle exit
73 , 73 a Welded or cast finished part
74 Transparent model
75 , 75 a reactor vessel
77 a-k manual valve
78 a-f solenoid valve
79 air collector
80 compressors
81 , 81 a cone container
82 , 82 a, 82 b, 82 c fluidized gas flow line
84 windbox
85 inclined shaft
87 , 87 a pyramidal reactor space
88 , 88 a pyramid container
α1 inclination angle
β1 angle of repose fine-grained bulk material
β2 angle of repose coarse-grained bulk material
γS shaft wall inclination
γD nozzle tilt
I, II, III, IV, V nozzle level
"A" detail
"B" detail

Claims (18)

1. fluidized bed reactor, consisting of a reactor vessel and an inclined shaft below, wherein in the oblique shaft wall in several nozzle planes above one another and staggered interspersed Wirbelgasöffnungen and can be equipped with nozzle inserts behind the oblique shaft wall provided a fluidizing gas supply and the shaft deepest a Wirbelgutabzug is connected, characterized that
  • a) nozzle rows ( 5 , 5 a, 5 b, 5 c, 5 d, 15 , 20 ) are inserted into the fluidizing gas openings of the nozzle planes (I, II, III, IV, V),
  • b) each of a plurality of individual nozzles ( 4 , 4 a, 4 b, 4 c, 4 d), which are connected to each other via a pressure equalization channel ( 11 ) consist, and
  • c) each nozzle plane (I, II, III, IV, V) is assigned its own windbox section ( 6 , 6 a, 6 b, 6 c, 6 d) of the vortex gas supply.
2. fluidized bed reactor according to claim 1, characterized in that the nozzle rows ( 15 , 5 b, 5 c, 20 ) from the uppermost nozzle level (V) to the lowermost nozzle level (I) with a decreasing number of individual nozzles ( 4 , 4 a , 4 b, 4 c) are fitted.
3 fluidized bed reactor according to claim 1, characterized in that the nozzle rows ( 5 ) in each nozzle plane (I, II, III, IV, V) with a constant number of one zeldüsen ( 4 , 4 a, 4 b, 4 c) equipped are.
4. fluidized bed reactor according to one of claims 1 to 3, characterized in that a plurality of nozzle rows ( 5 ) populated nozzle levels (I, II, III, IV) in the oblique shaft inner wall ( 22 ) are arranged.
5. fluidized bed reactor according to claim 4, characterized in that one or more with nozzle rows ( 5 ) be pieced nozzle levels (V) in addition in the container inner wall ( 22 a) are arranged.
6. fluidized bed reactor according to one of claims 4 or 5, characterized in that the Windkastenabschnitte ( 6 , 6 a, 6 b, 6 c) via fluidized gas flow conduits ( 82 , 82 a, 82 b, 82 c) and a valve register ( 28 ) Control valves ( 16 , 16 a, 16 b, 16 c) can be charged with fluidizing gas from a fluidizing gas line ( 53 ).
7. fluidized bed reactor according to one of claims 4 or 5, characterized in that the Windkastenabschnitte ( 6 , 6 a, 6 b, 6 c, 6 d) via a fluid gas line ( 53 a) with We belgas be charged and in the intermediate walls ( 30 ) Openings ( 61 , 61 a, 61 b, 61 c) are mounted with lei stungsmäßig tuned passage cross sections.
8. fluidized bed reactor according to one of claims 1 to 7, characterized in that the reactor vessel ( 75 ) and inclined shaft ( 2 ) consist of a heat-resistant steel wall ( 23 ).
9. fluidized bed reactor according to one of claims 1 to 7, characterized in that the reactor vessel ( 75 a) and inclined shaft ( 2 a) consist of a ceramic Isoliermassewand ( 24 ) and a Unterleg-sheet skin ( 34 ).
10. fluidized bed reactor according to one of claims 1 to 9, characterized in that the reactor vessel ( 75 , 75 a) as a round container ( 57 , 57 a) and the inclined shaft ( 2 , 2 a) as a cone container ( 81 , 81 a) are formed ,
11. fluidized bed reactor according to one of claims 1 to 9, characterized in that the reactor vessel ( 75 , 75 a) as a rectangular container ( 58 , 58 a) and the inclined shaft ( 2 , 2 a) as a pyramid container ( 88 , 88 a) are formed ,
12. fluidized bed reactor according to one of claims 1 to 7, characterized in that a nozzle row ( 5 ) of a heat-resistant steel wall ( 23 ) connected to the nozzle outlet plate ( 13 ), of a plurality of the intermediate wall ( 30 ) connected spacer plates ( 62 ) and from a plurality with the heat-resistant steel wall ( 23 ) and the intermediate wall ( 30 ) on the one hand and the nozzle outlet plate ( 13 ) on the other hand connected baffle ribs ( 63 , 63 a), which limit the nozzle holes ( 10 ) with the recess of a Druckaus gleichskanals ( 11 ).
13. fluidized bed reactor according to one of claims 1 to 7, characterized in that a nozzle row ( 5 ) consists of a with the lining sheet metal ( 34 ) and the ceramic Isoliermassewand ( 24 ) connected to the nozzle outlet plate ( 13 ), of a plurality of the intermediate wall ( 30 ) connected distance plates ( 62 ) and from several with the intermediate wall ( 30 ) and the ceramic Isoliermassewand ( 24 ) on the one hand and the nozzle outlet plate ( 13 ) on the other hand connected Leitchrichschrippen ( 63 , 63 a) consist, the nozzle holes ( 10 ) with recess a pressure equalization channel ( 11 ) zen limit.
14. fluidized bed reactor according to any one of claims 12 or 13, characterized in that the nozzle outlet plate ( 13 ) is inclined at an inclination angle (α1) from the horizontal downwards.
15. Fluidized bed reactor according to one of claims 1 to 7, characterized in that a nozzle row ( 5 ) from a welded or cast finished part ( 73 ) is formed, consisting of a nozzle outlet plate ( 13 ) and a nozzle cover plate ( 13 a), their individual nozzles (4, 4 a, 4 b, 4 c) of routing plate fins (63) or Leitblechrippen (63 a) with pressure compensation channel (11) are limited and the nozzle row (5) with the nozzle outlets (72) flush with the Inside wall surface ( 22 ) of the heat-resistant steel wall ( 23 ) is bindable ver.
16. fluidized bed reactor according to one of claims 1 to 7, characterized in that a nozzle row ( 5 ) of a welded or cast finished part ( 73 a) is formed, best starting from a nozzle outlet plate ( 13 ) and a Düsenab cover plate ( 13 a ), the individual nozzles (4, 4 a) of Leit plate fins (63) or Leitblechrippen (63 a) with pressure compensation channel (11) are limited, and the nozzle row (5) flush with the inner wall surface (22) of the Kera mix Isoliermassewand ( 24 ) is connectable.
17. fluidized bed reactor according to claim 7, characterized in that in the fluidized gas line ( 53 a), a burner ( 27 ) is integrated for vortex gas preheating.
18. fluidized bed reactor according to one of the preceding claims, characterized in that the individual nozzles ( 4 ) of the nozzle rows ( 5 ) are arranged downwardly and laterally inclined to produce an angular momentum and to set the firing stoves in rotation.
DE19924217110 1992-05-22 1992-05-22 Fluidised bed reactor with inclined shaft Ceased DE4217110A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
DE19924217110 DE4217110A1 (en) 1992-05-22 1992-05-22 Fluidised bed reactor with inclined shaft

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19924217110 DE4217110A1 (en) 1992-05-22 1992-05-22 Fluidised bed reactor with inclined shaft
PCT/EP1993/001255 WO1993024218A1 (en) 1992-05-22 1993-05-20 Fluidised bed reactor with oblique shaft

Publications (1)

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DE4217110A1 true DE4217110A1 (en) 1993-11-25

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WO (1) WO1993024218A1 (en)

Cited By (1)

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Publication number Priority date Publication date Assignee Title
EP1025899A1 (en) * 1999-02-03 2000-08-09 Herbert Hüttlin Particulate material processing apparatus

Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
DE102011117811A1 (en) * 2011-11-07 2013-05-08 H S Reformer Gmbh Fluidized bed reactor

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Publication number Priority date Publication date Assignee Title
DE1442613A1 (en) * 1962-06-22 1968-11-14 Coal Industry Patents Ltd Method and apparatus for fluidizing coal eg

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DE1071056B (en) *
DE3523653C2 (en) * 1985-07-02 1989-08-03 Asea Brown Boveri Ag, 6800 Mannheim, De

Patent Citations (1)

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Publication number Priority date Publication date Assignee Title
DE1442613A1 (en) * 1962-06-22 1968-11-14 Coal Industry Patents Ltd Method and apparatus for fluidizing coal eg

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1025899A1 (en) * 1999-02-03 2000-08-09 Herbert Hüttlin Particulate material processing apparatus
US6367165B1 (en) 1999-02-03 2002-04-09 Huettlin Herbert Device for treating particulate product

Also Published As

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WO1993024218A1 (en) 1993-12-09

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