TW201347851A - Centrifugal separator - Google Patents

Abstract

This invention is related to a method and a device for optimizing a centrifugal separator, especially a feedback cyclone separator of a high temperature carburetter in order to significantly increase the separation efficiency of a centrifugal separator. This is achieved by increasing a local of centrifugal force at a dip tube of the centrifugal separator.

Description

Centrifugal separator

The present invention relates to a method of optimizing a centrifugal separator, and more particularly to a method of optimizing a feedback cyclone separator of a high temperature gasifier.

Centrifugal separators come in a variety of different shapes. For example, DE 103 46 692 A1 proposes a droplet separator having an insertion tube swirling vane at the outer edge of the transition zone leading to the funnel zone so that the gas flow into the funnel forms a rotation within the funnel. For example, DE 102 05 981 A1 proposes a cyclone which can be switched on and off, while DE 195 16 817 C1 proposes a cyclone with an element (for example a corona electrode).

The purpose of developing a high-temperature gasifier is to increase the efficiency of lignite use through a fluidized bed gasification process, which is a so-called high-temperature Winkler gasifier (HTW) that is further improved by a Winkler coal gasifier that was originally operated at ambient pressure. ). The advantages of this method are mainly due to higher raw material use efficiency, greatly increased gasification capacity of large equipment, and avoidance of by-product formation.

The disadvantage of this method is that since the separation efficiency of the feedback cyclone is not high, it is necessary to install an expensive hot gas filter behind the cyclone and the raw material gas cooler. Another disadvantage is that The dust separated in the hot gas filter also contains a large amount of carbon. This dust cannot be buried, but must be sent back to the gasifier via a pipeline and a screw conveyor, or it can be sent to a separate boiler to assist in fuel combustion.

The object of the present invention is to substantially increase the separation rate of the centrifugal separator, and in particular to greatly increase the separation rate of the feedback cyclone separator of the high temperature gasifier.

According to one embodiment of the present invention, it is only necessary to locally increase the centrifugal force at the insertion tube of the centrifugal separator, so that the above-described object can be attained by the method described at the beginning of the invention.

In order to increase the efficiency of the cyclone separator, a known method is to move the insertion tube into the "dead water zone", that is, the insertion tube is eccentrically mounted into the cyclone. It is only economical to take such measures when manufacturing a new cyclone. After-the-fact modification and after-the-fact optimization are not economically viable. Conversely, locally increasing the centrifugal force at the insertion tube is an after-the-fact measure that can be taken without difficulty.

One embodiment of the invention is to install a coalescer in the input zone of the centrifugal separator to mechanically increase the particle size of the particles to be separated. The size of the particles can be influenced by the agglomerator to increase the collision rate between the large particles and the small particles in the input region of the cyclone, and the separation rate is significantly improved. Coagulation devices are known devices, such as the coagulation device disclosed in DE 198 15 976 A1.

Since the cyclone separators operate perfectly only when they are in close proximity to each other, for example, the dust is at the optimum tangent incidence speed. It is 10m/s into the cyclone, and the efficiency of the cyclone changes when the load changes. To this end, the present invention optimizes such cyclones by varying the cross-section of the input section of the centrifugal separator. As will be described below, there are a number of different ways in which the differences can be made for cross-sectional changes.

The variable section can be used to keep the design (calculation) speed of the cyclone constant.

One embodiment of the invention is to employ several of the above mentioned measures simultaneously.

In order to attain the objects of the present invention, the present invention also provides a device and/or a centrifugal separator characterized in that a fluid guiding member for narrowing the fluid passage of the centrifugal separator is provided at the insertion tube. In the present invention, such a fluid guiding member that narrows the fluid passage may be constituted by a disc-shaped guide spacer.

According to the invention, in order to achieve a particularly optimized flow, an eccentric disc-shaped guide diaphragm can be arranged on the outside of the insertion tube opposite the gas inlet, wherein the extent of the guide partition extends below the lower edge of the gas inlet passage, It is then narrowed to match the shape of the tube at the bottom end of the insertion tube. The position of the guide partition can vary depending on the shape of the centrifugal separator.

According to the invention, in order to mechanically enlarge the particle size, an agglomerator can be provided in the input region of the centrifugal separator, the agglomerator being constituted by a plurality of tubular flow disturbing elements passing through the fluid passage. These tubular flow disrupting elements can be mounted into the fluid passage in a vertical, parallel or inclined manner.

As described above, in order to keep the design (calculation) speed of the cyclone constant even when the load is replaced, one embodiment of the present invention provides a fluid input channel with a movable wall or ceramic that changes the channel section. A shutter, wherein in accordance with an embodiment of the invention, the horizontal or vertical movable wall is constructed of a shutter or a baffle member that is curved toward the centrifugal separator in the transition zone.

1‧‧‧ gasifier

2‧‧‧storage tank

3‧‧‧Sediment discharge

4‧‧‧Spiral conveyor

5‧‧‧ centrifugal separator

6, 7‧‧‧ pipeline

8, 11, 12‧‧ arrows

9‧‧‧Insert tube

10, 10a‧‧‧ fluid-directed partition

13‧‧‧ agglomerator

14‧‧‧ Input channel

15‧‧‧Mobile interference components

16‧‧‧ceramic ram

17, 19, 21, 23‧‧‧ double arrows

18, 20, 22‧‧‧ ceramic plates

Figure 1 is a simplified diagram of a high temperature Winkler gasifier.

Figures 2 through 7 are simplified diagrams of a centrifugal separator having different flow altering members.

The features, details and advantages of the present invention will be further described below in conjunction with the drawings.

Figure 1 is a simplified diagram of a high temperature Winkler gasification system comprising a gasifier 1 for inputting material via a sump 2. The deposit is discharged from the sediment discharge port 3, for example, by using a screw conveyor 4. The gas will impact the centrifugal separator 5, where the solid particles will return to the gasifier 1 via line 6, and the gas will be discharged via line 7 for further processing.

Figures 2 through 7 show various ways of affecting the flow in the centrifugal separator 5: arrow 8 in Figure 2 represents the introduction of a mixture of solids and gases into the centrifugal separator 5, wherein the mixture flows around the insertion tube 9. .

In order to accelerate the fluid, the insertion tube 9 carries a flow disrupting element 10, wherein the flow disrupting element is a curved guiding partition which is welded or otherwise fixed to the insertion tube 9. As can be seen from Fig. 2, the bottom portion 10a of the guide partition 10 is narrowed so that the original sectional area of the fluid passage is again reached at the trailing end of the insertion tube 9. As indicated by arrow 11, the purified gas leaves the centrifugal separator 5 via line 7. As indicated by arrow 12, the solid particles exit the centrifugal separator downward.

For better display, Fig. 2 shows the guide plate 10 having the narrowed section 10a displayed at a predetermined position. However, this location does not necessarily have to match the actual installation location.

In the following drawings, all elements that are the same as in the first embodiment are denoted by the same reference numerals, and the arrows are the same.

As can be seen from Fig. 3, the embodiment of Fig. 3 differs from Fig. 2 in that, in order to form the agglomerator 13, a tubular flow disturbing element 15 is mounted in the input passage 14 of the centrifugal separator 5, and As with the horizontal mounting shown in Figure 3, the flow disrupting element 15 can also be mounted in the input channel 14 in a vertical or diagonal manner.

According to the embodiment of Fig. 4, the section of the input passage 14 of the centrifugal separator 5 can be changed by a lifting and/or lowering blocking member or ceramic shutter 16. A double arrow 17 shows the movement of the blocking element or ceramic shutter.

In the embodiment of Figure 5, the cross-section of the input channel 14 of the centrifugal separator 5 can be varied by a raised and lowered bottom plate (e.g., a bottom plate constructed of a ceramic plate), wherein the double arrow 19 indicates the possible bottom plate 18. mobile.

In the embodiment of Fig. 6, the ceramic plate 20 can be vertically oscillated to change the cross section of the input passage, wherein the double arrow 21 indicates the movement of the ceramic plate.

Figure 7 shows another method of reducing the cross-section of the input zone of the centrifugal separator 5 by using a plate 22 that cooperates with the curved wall of the centrifugal separator, with the double arrow 23 showing the movement of the plate.

As previously described herein, the results of the individual measures can also be used together, i.e., on the one hand, the cross-section of the input channel 14 is altered by a suitable ceramic plate 18, 20 or 22, along with the agglomerator 13 and the fluid-guiding baffle 10. , 10a.

1‧‧‧ gasifier

2‧‧‧storage tank

3‧‧‧Sediment discharge

4‧‧‧Spiral conveyor

5‧‧‧ centrifugal separator

6, 7‧‧‧ pipeline

14‧‧‧ Input channel

Claims (10)

A method for optimizing a centrifugal separator, which is a method for optimizing a feedback cyclone separator of a high temperature gasifier, characterized in that the centrifugal force is locally increased at the insertion tube of the centrifugal separator. A method for optimizing a centrifugal separator, which is a method for optimizing a feedback cyclone separator of a high temperature gasifier, characterized in that a agglomerator is installed in an input region of the centrifugal separator to mechanically increase particles to be separated Particle size. A method for optimizing a centrifugal separator, which is a method for optimizing a feedback cyclone separator of a high temperature gasifier, characterized in that the section at the input of the centrifugal separator is changed. A method for optimizing a centrifugal separator, which is a method for optimizing a feedback cyclone separator of a high temperature gasifier, characterized in that several measures such as the first to third items of the patent application are taken at the same time. A device for carrying out the method of claim 1, characterized in that a fluid guiding element (10) for narrowing the fluid passage of the centrifugal separator (5) is provided at the insertion tube (9). A device according to claim 5, wherein a disc-shaped guide partition (10) for narrowing the fluid passage of the centrifugal separator (5) is provided outside the insertion tube (9). The apparatus of claim 6, wherein the eccentric disc-shaped guide partition (10) that narrows the fluid passage of the centrifugal separator (5) outside the insertion tube (9) is located opposite the gas inlet. The extent of the guide partition (10) extends below the lower edge of the gas inlet passage (14) and then narrows to match the shape of the tube at the bottom end of the insertion tube. A device for carrying out the method of claim 2, characterized in that the agglomerator (13) located in the input channel (14) of the centrifugal separator (5) is a plurality of tubular flow interference elements passing through the fluid channel ( 15) Composition. A device for carrying out the method of claim 3, characterized in that the input channel (14) is provided with a movable wall or ceramic shutter (16) which changes the cross section of the channel. A device according to claim 9 wherein the horizontal or vertical movable wall (16, 18, 20) is formed by a shutter or a baffle member (22) which is bent toward the centrifugal separator in the transition zone.