METHOD AND DEVICE FOR PROCESSING FLUE DUST

Abstract

The method and the device serve to treat the flue dust formed during the production of nonferrous metals. After the addition of sulfur and/or a sulfur compound, the flue dust is heated, and volatile compounds are separated in a downstream offgas treatment unit. The flue dust is heated in an inert atmosphere.

Claims

1. A method for processing flue dust formed during production of copper based on a smelting process of copper ores, the method comprising the steps of: adding sulfur and/or a sulfur compound to the flue dust; heating the flue dust in an inert atmosphere after the addition of the sulfur and/or sulfur compound; and separating volatile components, the flue dust being subjected to a pyrometallurgical treatment in a fluidized bed reactor in which the flue dust is heated in an inert atmosphere, the pyrometallurgical treatment producing an offgas that is subjected to an offgas treatment for removing arsenic-sulfur compounds as volatile elements, wherein treatment of the flue gas is carried out as a continuous process.

2. The method according to claim 1, including volatilizing arsenic in elementary form or in form of arsenic-sulfur compounds and then separating the arsenic or arsenic-sulfur compound from the flue dust.

3. The method according to claim 1, including processing the flue dust at ambient pressure.

4. The method according to claim 1, including carrying out the treatment of the flue dust at a negative pressure.

5. The method according to claim 1, including carrying out the treatment of the flue at a positive pressure.

6. The method according to claim 1, wherein an average amount of sulfur dioxide in the offgas is no greater than 5 vol. %.

7. The method according to claim 1, wherein the heating of the flue dust includes heating the flue dust at least temporarily to a temperature in the range of 500-1,000 C.

Description

BRIEF DESCRIPTION OF THE DRAWING

[0025] In the drawings:

[0026] FIG. 1 shows the concept of a system for the pyrometallurgical treatment of flue dust in a rotary kiln with a two-stage offgas treatment;

[0027] FIG. 2 shows the concept of a method for the pyrometallurgical treatment of flue dust in the fluidized-bed process with a one-stage offgas treatment;

[0028] FIG. 3 shows a diagram of the removal of flue dust; and

[0029] FIG. 4 shows a sulfur balance for comparison of the prior art with the inventive method.

DETAILED DESCRIPTION OF THE INVENTION

[0030] FIG. 1 shows the use of a rotary kiln 1, in which the supplied material is treated at a temperature of approximately 900 C. The supplied materials consist in this case of a copper concentrate and separated flue dust. The dust is separated in the area of a cyclone 2.

[0031] The treatment in the rotary kiln 1 proceeds in an inert atmosphere. Typically, nitrogen is used for this. When the mixture of concentrate and flue dust is supplied at a mass flow rate of 300 tons per day, nitrogen will typically be supplied at a rate of 15,000 Nm3 per hour. At this level of throughput, the amount of offgas supplied to the cyclone 2 will typically be 20,000 Nm3 per hour at an offgas temperature of approximately 900 C. (Nm3=normal cubic meter).

[0032] Other gases can be used as an alternative to nitrogen as the inert gas. For example, the use of argon is possible. The grate temperature of 900 C. represents merely a preferred temperature. It is typically possible to realize a temperature in the range from 650 C. to 950 C. The flue dust and the fresh concentrate are supplied to the rotary kiln 1 in a concentrate-to-flue dust mixing ratio typically in the range of 1:3-1:1. The residence time of the mixture in the rotary kiln 1 is typically 1-4 hours.

[0033] Downstream from the cyclone 2, a separator 3 is installed, in which an arsenic-containing solid is collected. Offgas from the separator 3 is sent to a secondary separator 4. For energy recovery, the secondary separator 4 is provided with a heat exchanger 5 to reduce the temperature of the final offgas to about 40 C. and to make use of the available energy.

[0034] All of the values for the process parameters in FIG. 1 are given merely as examples and can be varied over a considerable range. The method can thus be adapted to the concrete requirements of the application, to the throughputs, and to the nature of the starting products.

[0035] FIG. 2 shows a modification of the concept according to FIG. 1. Instead of the rotary kiln 1, a fluidized-bed system 6 is used. The separator 3 and the secondary separator 4 are combined into a one-stage separator 7. By the use of the heat exchanger 5, the temperature of the final offgas can be suitably reduced with this concept as well.

[0036] FIG. 3 illustrates in general terms how the flue dust is handled and discharged during copper production.

[0037] FIG. 4 illustrates a sulfur balance for comparison of the prior art with the inventive concept of the method for a selected throughput example.

[0038] The inventive separation and treatment of the flue dust is preferably conducted as a continuous process. Also preferred is a process conducted at ambient pressure. The process can also be conducted, however, at a negative pressure or at a positive pressure, depending on the concrete requirements of the application.

[0039] The inventive treatment of the flue dust in an inert atmosphere takes especially into account the fact that arsenic or other substances to be removed from the flue dust are typically in a form different from that of the underlying concentrate. Comparison shows that the distribution coefficients and other chemical bonds in the flue dust are typically different from those in the concentrate. For example, the arsenic in the concentrate can be in the form of enargite, tennantite, arsenopyrite, or arsenic sulfide; whereas, in the flue dust, the arsenic is typically in the form of arsenic oxide, arsenic sulfide, and iron or copper arsenate.

[0040] The inert atmosphere during the roasting process makes it possible to achieve a significant lowering of the SO2 content in the offgas. What is aimed for here is an SO2 content below 5 vol. %, preferably below 2 vol. %. As an option, it is also possible to oxidize the offgas or certain portions of the offgas.

[0041] While specific embodiments of the invention have been shown and described in detail to illustrate the inventive principles, it will be understood that the invention may be embodied otherwise without departing from such principles.