METHOD AND INSTALLATION FOR GASIFICATION OF HETEROGENIC MIXTURES OF ORGANIC SUBSTANCES AND COMPOUNDS

Abstract

The present invention relates to a process and an installation for the continuous flow of gasification of heterogeneous mixtures of organic substances and compounds such as biomass waste, forestry, municipal solid and liquid waste, sludge from sewage treatment plants and other similar waste. The process has the following steps: a) the organic raw material in heterogeneous mixture is introduced into the pyrolysis reactor where it is gradually heated, by forced convection and thermal radiation, to a temperature of 900 . . . 1000 C., being kept in contact with metal surfaces that transport thermal energy through conduction from the exothermic area of the gasification reactor. The metal surfaces are placed in fixed positions, different so that the contact surface changes after 5 . . . 20 cm traversed by the flow of organic raw material, each group of metal slats forming 2 . . . 8 separation planes, b) the results the pyrolysis process, respectively the solid, liquid and gaseous phases, are gravitationally transferred to the gasification reactor (1) where they are mixed with the gasification agent, respectively air/oxygen and steam in two successive enclosures, the first enclosure with vortex flow and the second with laminar flow, each stage having independent control of the process parameters. The installation according to the invention consists of one or more pyrolysis reactors (2) of cylindrical or prismatic shape, fixed in the enclosures (15) of the gasification reactor (1), a nozzle system (18) for the controlled introduction of air/oxygen and a lock system consisting of the valve (3) and the container (4) for slag removal.

Claims

1. Installation for the treatment of heterogeneous mixtures of solid and liquid organic substances and compounds by gasification, characterized in that it consists of: one or more fixed pyrolysis reactors, positioned in appropriate enclosures created in the gasification reactor, so that by metal-to-metal contact to create metal thermal bridges, as they are defined in the description of the invention, to transport thermal energy from the exothermic zone of the gasification reactor in the endothermic zone of the pyrolysis reactor a gasification reactor in which the pyrolysis products are gravitationally transferred and processed in two successive chambers, the first with vortex flow and the second with laminar flow of the gasifying agent, respectively air/oxygen and steam.

2. Installation according to claim 1, characterized in that the cylindrical or prismatic pyrolysis reactor, preferably cylindrical in shape, has 4-14 groups of metal slats with a height of 5-20 cm inside, positioned transversely by welding to the outer walls., preferably 10 cm, so that the separation plans made by each group are different from the separation plans of the adjacent groups.

3. Installation according to claim 1, characterized in that the gasification reactor has no bed of organic raw material.

4. Installation according to claim 1, characterized in that the gasification reactor contains a nozzle system for introducing air/oxygen and steam so that an upward eddy current is produced in the vortex chamber which will increase the residence time of the pyrolysis products and will increase the efficiency of carbon oxidation.

Description

BRIEF DESCRIPTION OF DRAWINGS

[0053] Below is a practical example of installation for the application of the process described in connection with drawings 1-4 which represent:

[0054] FIG. 1 Pyrolysis and Gasification Reactor Assembly

[0055] FIG. 2 Pyrolysis Reactor

[0056] FIG. 3 Gasifier Reactor

[0057] FIG. 4 Central Part of the Gasifier Reactor

EXAMPLES

[0058] The pyrolysis reactor shown in drawing 2 is a reactor with an inside diameter of 240 mm that can process 0.8-1 tons/hour of municipal solid waste from non-hazardous and hazardous categories regardless of the percentage of water contained. The reactor contains 8 sets of metal slats with a height of 10 cm welded to the outer cylindrical wall to take over the thermal energy by conduction and achieve thermal transfer by convection to the organic raw material. The total contact area of the 8 sets of blades amounts to 1.6 m.sup.2. Between the sets of slats is a distance of 4 cm for the resettlement and homogenization of the flow of organic material. In our own experiments we tested speeds of movement of organic materials from 10 to 30 mm/s. A relatively uniform temperature distribution was obtained on the contact slats, from 100 C at the inlet to the reactor at 800 C on the last set of slats, a phenomenon that can be explained due to the supply and distribution system of thermal energy and energy absorbed by matter. organic premium introduced in the process.

[0059] The gasification reactor 1 has an original shape, adapted to the process and the new functional conditions, presented in FIG. 3, composed of the upper part 11, the central part 12 and the lower part 13, with details of the central part presented in FIG. 4.

[0060] The rest of the gasifier, the grate 14 (fixed or mobile), the slag evacuation and the syngas evacuation are common elements according to the known techniques. The complete gasification reactor is made with double jacket for cooling with water/steam, made of stainless steel without internal thermal insulation. Outside, the reactor is covered with thermal insulation made of mineral wool to reduce the loss of thermal energy outside.

[0061] This gasification reactor with an inner diameter of 2 m, equipped with 2 pyrolysis reactors with an inner diameter of 240 mm, has a processing capacity of about 2 tons per hour mixture of organic materials from non-hazardous and/or hazardous categories, with water content up to 50% mass percentage. Depending on the end use of the synthesis gas, for the production of electricity, liquid fuels, fertilizers or hydrogen, the amount of air and steam can be controlled to obtain an H2/CO ratio between 0.9 and 100. The minimum oxidation efficiency of carbon is of 90%.