PROCESSING OF OFF-GAS FROM WASTE TREATMENT

Abstract

Waste treatment comprises heating it in a chamber to effect pyrolysis of the waste, introducing oxygen into the chamber to effect combustion of the pyrolyzed waste, and contacting off-gas from the pyrolysis and/or combustion steps with an oxidation catalyst to convert carbon monoxide and hydrocarbons in the off-gas into carbon dioxide and water and with a reduction catalyst to convert nitrous oxides to nitrogen and oxygen. Thus, domestic waste is treated in a batch process using catalytic converters to reduce the level of toxic components before off-gas reaches the atmosphere.

Claims

1-44. (canceled)

45. A method for treatment of a waste, comprising: heating the waste in a chamber to an elevated temperature to effect pyrolysis of the waste; introducing oxygen into the chamber to effect gasification of the pyrolyzed waste such that pyrolysis and gasification are carried out in sequence in the same chamber, wherein an off-gas is produced; contacting off-gas from the pyrolysis and/or gasification steps with an oxidation catalyst to convert carbon monoxide and hydrocarbons in the off-gas into carbon dioxide and water; measuring the oxygen content of an exhaust gas from the oxidation catalyst using an oxygen sensor, and using this information to modulate an air input to the oxidation catalyst or to the chamber or to both the oxidation catalyst and the chamber so as to maintain the oxygen level of a gas exiting an apparatus comprising the chamber and the oxidation catalyst; and monitoring the oxidation catalyst temperature using a temperature sensor in or near the oxidation catalyst so that an increase in temperature triggers an increase in the air input to the oxidation catalyst to reduce the temperature.

46. The method according to claim 45, wherein the elevated temperature to effect pyrolysis is from 400-700 C.

47. The method according to claim 45, wherein the oxygen level of the gas exiting the apparatus is maintained within the 1-16% range.

48. The method according to claim 45, wherein the oxygen level of the gas exiting the apparatus is maintained within the 3-10% range.

49. The method according to claim 45, wherein the oxidation catalyst comprises platinum, palladium or rhodium.

50. The method according to claim 45, wherein an increase in the oxidation catalyst temperature above about 600 triggers an increase in the air input to the oxidation catalyst.

51. The method according to claim 45, further comprising contacting the off-gas with a reduction catalyst to convert nitrous oxides into nitrogen and oxygen.

52. The method according to claim 51, wherein the reduction catalyst comprises platinum, palladium or rhodium.

53. The method according to claim 45, further comprising contacting the off-gas with a wet scrubber to remove inorganic acids and volatile metals.

54. The method according to claim 51, further comprising filtering the off-gas to remove ash prior to the contact of the off-gas with the oxidation and/or reduction catalysts.

55. The method according to claim 54, comprising contacting the off-gas with a cyclone to remove ash prior to the contact of the off-gas with the oxidation and/or reduction catalysts.

56. The method according to claim 45, further comprising passing the exhaust gas from the oxidation catalyst through a heat exchanger.

57. A waste treatment apparatus, comprising: a chamber to receive a waste; a heater to heat the waste in the chamber; an outlet for exit of an off-gas from the chamber; an oxidation catalyst to catalyse oxidation of carbon monoxide and hydrocarbons in the off-gas; and characterized in that it also comprises: an oxygen monitor to monitor the oxygen content of an exhaust gas from the oxidation catalyst; an input to combine air with the off-gas prior to contact with the oxidation catalyst, wherein the input of air into the off-gas prior to contact with the oxidation catalyst is controlled by the oxygen monitor; and a temperature sensor for monitoring the operating temperature of the oxidation catalyst, wherein the temperature sensor is connected to the air input such that the input of air can be controlled to modulate the operating temperature of the oxidation catalyst, the apparatus adapted to be sealed so that the waste can be heated to effect pyrolysis of the waste and comprising an inlet for air to enable gasification of the waste in the same chamber.

58. The apparatus according to claim 57, adapted to effect pyrolysis of the waste at a temperature from 400-700 C.

59. The apparatus according to claim 57, adapted such that the contact with the oxidation catalyst is controlled by the oxygen monitor such that the oxygen content of the off-gas after the contact with the oxidation catalyst is within the range of 1-16%.

60. The apparatus according to claim 57, adapted such that the contact with the oxidation catalyst is controlled by the oxygen monitor such that the oxygen content of the off-gas after the contact with the oxidation catalyst is within the range of 3-10%.

61. The apparatus according to claim 57, wherein the oxidation catalyst comprises platinum, palladium or rhodium.

62. The apparatus according to claim 57, further comprising a reduction catalyst to catalyse reduction of nitrous oxides in the off-gas.

63. The apparatus according to claim 62, wherein the reduction catalyst comprises rhodium.

64. The apparatus according to claim 62, further comprising an ash filter between the chamber and the oxidation and/or reduction catalysts to prevent ash in the off-gas reaching the oxidation and/or reduction catalysts.

65. The apparatus according to claim 64, comprising a cyclone to prevent ash entering the oxidation and/or reduction catalysts.

66. The apparatus according to claim 57, further comprising a heat exchanger to process the exhaust gas exiting the oxidation catalyst and entering the chamber.

Description

[0055] The invention is now illustrated with reference to the accompanying figures in which:

[0056] FIG. 1 shows a schematic flow-diagram of a first embodiment of the invention using an oxidation catalyst;

[0057] FIG. 2 shows a schematic flow-diagram of a second embodiment of the invention using an oxidation catalyst;

[0058] FIG. 3 shows a schematic flow-diagram of a third embodiment of the invention using an oxidation catalyst;

[0059] FIG. 4 shows a schematic flow-diagram of a fourth embodiment of the invention using an oxidation catalyst and a reduction catalyst;

[0060] FIG. 5 shows a schematic flow-diagram of a fifth embodiment of the invention using a single oxidation catalyst; and

[0061] FIG. 6 shows a schematic flow-diagram of a sixth embodiment of the invention using a single catalyst in combination with a heat exchanger and feedback control of oxygen levels and catalyst temperature.

EXAMPLES

[0062] Apparatus not specifically described is as described previously in the International patent application published as WO2007/104954, also referred to herein as the PyroPure apparatus, the contents of which are incorporated herein by reference.

[0063] Referring to FIG. 1, the PyroPure chamber operates at temperatures from 0 C. up to about 600 C., generally at about 550 C. and the off-gases pass into a diesel particulate filter, DPF. This operates at about 550 C.-850 C., generally at about 750 C. and removes tar from the gas. Air is input at that stage to enable catalytic oxidation to take place, control of air flow controlling the catalyst temperature.

[0064] The output of the DPF is passed to a VTT unit, a VOC thermal treatment unit which operates at about 1000 C. This destroys H.sub.2, volatile organic compounds and heavy tars, however, it can produce some thermal NO.sub.x. Thus, it produces an output which may have to be dealt with subsequently, though NO.sub.x remains in general below acceptable limits in which case no specific treatment is needed. From the VTT the gases pass to a wet scrubber operating at about 80 C. in which the gas exits below the water level and passes up through a water mist. This removes remaining tar (if any) and soluble gases such as SO.sub.2 and HCl. Next, the gas passes through a dry filtration unit, a mist eliminator operating at above 120 C. to prevent condensation, which prevents carry over of water vapour into subsequent processing stages. The gases now pass through a ceramic filter which operates at about 200 C. and eliminates remaining particulates. This filter is omitted if the eventual output passes into the sewer water, as the sewer water will also remove particulates, and is therefore not shown in FIG. 1.

[0065] The water scrubber contains approximately 40 litres of water and is a closed unit, the water continuously circulating through it during the cycle time. At the end of the cycle the water is flushed out into the sewer. The pH of the water in the scrubber should be in the region of 6-7, i.e. neutral, and with the majority of waste loads this will be maintained. However it is possible that with a load with a high PVC content the pH value will drop and the water will become too acidic. The pH value is measured during the process and if it begins to drop more water is added. Fresh water can also be continuously added whilst waste water is removed.

[0066] The next stage is a so-called auto cat, meaning a conventional 2-way catalytic converter of the type available in the automobile industry. Heated air is input at this stage and the catalytic converter typically operates at about 400 C. This removes CO together with some VOCs.

[0067] Finally, the treated gas passes through a carbon filter (not shown in FIG. 1) operating at less than 100 C., the gas finally exiting at temperatures below 50 C. in accordance with the existing legislation.

[0068] The output contains contaminants at levels which are acceptable according to the current environmental legislation. This enables the output to go into the atmosphere and/or into the sewer so that the equipment can operate in situ.

[0069] FIG. 2 shows an adaptation of the FIG. 1 embodiment, in which the VTT is dispensed with. This means there are fewer NO.sub.x contaminants as none are generated by the VTT of the FIG. 1 embodiment.

[0070] The DPF removes tar and a fraction of VOCs and CO via catalytic oxidation. The wet scrubber, operating at about 70 C., removes inorganic acids and volatile metals and the dry filtration removes particulates not caught by the wet scrubber. The final catalytic bed is an HT catalyst, capable in particular of removing VOCs such as methane and ethane from the off-gas (removed in the FIG. 1 embodiment by the VTT) and operates at about 600 C. and removes VOCs, CO and hydrogen.

[0071] This embodiment relies on minimizing nitrous oxide formation thus avoiding the need for a reduction catalyst.

[0072] FIG. 3 shows an adaptation of the FIG. 2 embodiment, in which the wet scrubber is positioned after the second catalytic bed.

[0073] As with FIG. 1, the DPF removes tar and a fraction of VOCs and CO via catalytic oxidation. Off-gas then passes into the second catalytic bed, an HT catalyst, into which air, optionally heated air is input and operating at about 600 C. This completes oxidation of CO and VOCs and hydrogen to carbon dioxide and water.

[0074] Gases then pass to the wet scrubber, operating at about 70 C., which removes inorganic acids, volatile metals and particulates, the latter with such efficiency that a separate dry filtration is not needed. After the water scrubber the cleaned and filtered air with an oxygen content generally from 10%-21% is vented into the sewer pipe.

[0075] A further embodiment of the invention is shown at FIG. 4. As for the other embodiments, off-gas passes first through a DPF oxidation catalyst. From here the gases pass through a 3-way catalytic converter, which can act as reduction catalyst to reduce nitrous oxides and then into the catalytic bed of an HT oxidation catalyst, with input of air, where oxidation of VOCs and CO is completed. Lastly, the gases pass through the wet scrubber. After the water scrubber the cleaned and filtered air with an oxygen content generally from 10%-21% is vented into the sewer pipe.

[0076] A still further embodiment of the invention is shown at FIG. 5. Off-gas exiting the chamber passes through a metal mesh filter (not shown) to remove ash and then does not pass through a DPF as in other embodiments but through a catalytic bed of an HT catalyst where, with input of air, oxidation of tar, VOCs and CO is carried out. Lastly, the gases pass through the wet scrubber. After the water scrubber the cleaned and filtered air with an oxygen content from 10%-21% is vented into the sewer pipe.

[0077] A preferred embodiment of the invention is shown at FIG. 6. Pyrolysis, combustion (gasification) and off-gas treatment are substantially as per previous examples, unless otherwise stated. Raw exhaust gases exiting the chamber first pass through a cyclone to remove ash from the off-gas prior to contact of off-gas with a catalyst. In this apparatus the catalyst is a palladium/alumina oxidation catalyst having a single catalyst bed. Exiting the cyclone, off-gases then pass through the catalyst bed and a thermocouple associated with the catalyst provides temperature feedback information to a variable air blower. The air blower controls the amount of air to be mixed with the exhaust gases and this air is first passed though a heater to modulate its temperature. Exhaust gases exiting the catalyst bed pass through a heat exchanger en route to the gas scrubber. The heat exchanger transfers heat from the catalyst bed exhaust onto air injected into the chamber that is used during the pyrolysis and oxidation stages. Cooled exhaust gases exiting the heat exchanger pass through the gas scrubber for removal of SO.sub.2, acids, particulates and volatile metals and are cooled still further by the water in the scrubber. Clean exhaust gases exiting the scrubber pass via an oxygen detector which monitors the oxygen content in the exhaust gas and provides feedback information to the variable air blower in order to further modulate the amount of air being mixed with the exhaust gases input to the oxidation catalyst.

[0078] In one operation of the apparatus, about 8 kg of typical household waste is placed in the chamber, which is heated to about 550 C. for pyrolysis with an airflow of about 16 L/min introduced from the start. The pyrolysis stage lasts for about 40 minutes after which air flow into the chamber is increased gradually up to about 150 L/min, starting the oxidation stage. When the pyrolysis stage begins the catalyst bed is heated to about 600 C. by heated air being supplied from the variable air blower at a rate of about 200 L/min. The air flow is increased up to about 800 L/min during the run as required. The rate of air flow is controlled by the thermocouple maintaining the temperature of the catalyst within its operating temperature and the oxygen content of the final exhaust gas as measured by the oxygen detector. The oxygen content of the final exhaust gas is controlled within the 3-10% range.

[0079] The invention thus provides waste treatment method and apparatus.