PH12017000201A1 - Multi-stage waste remediation system - Google Patents
Multi-stage waste remediation system Download PDFInfo
- Publication number
- PH12017000201A1 PH12017000201A1 PH12017000201A PH12017000201A PH12017000201A1 PH 12017000201 A1 PH12017000201 A1 PH 12017000201A1 PH 12017000201 A PH12017000201 A PH 12017000201A PH 12017000201 A PH12017000201 A PH 12017000201A PH 12017000201 A1 PH12017000201 A1 PH 12017000201A1
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- Philippines
- Prior art keywords
- chamber
- waste
- tank
- moisture
- heating
- Prior art date
Links
- 239000002699 waste material Substances 0.000 title claims abstract description 79
- 238000005067 remediation Methods 0.000 title abstract description 10
- 238000010438 heat treatment Methods 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 18
- 238000004075 wastewater filtration Methods 0.000 claims abstract description 5
- 239000000446 fuel Substances 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 claims description 3
- 230000003416 augmentation Effects 0.000 claims description 2
- 238000005868 electrolysis reaction Methods 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 9
- 238000005979 thermal decomposition reaction Methods 0.000 abstract description 6
- 239000010805 inorganic waste Substances 0.000 abstract description 4
- 239000010815 organic waste Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000005336 cracking Methods 0.000 description 4
- 239000002910 solid waste Substances 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000004568 cement Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000005204 segregation Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000011217 control strategy Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 201000010099 disease Diseases 0.000 description 1
- 208000037265 diseases, disorders, signs and symptoms Diseases 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000008029 eradication Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000002459 sustained effect Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/02—Multi-step carbonising or coking processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/007—Screw type gasifiers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/62—Processes with separate withdrawal of the distillation products
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1684—Integration of gasification processes with another plant or parts within the plant with electrolysis of water
Abstract
The present invention relates to waste remediation processes, in particular to a self-sustained multi-stage thermal decomposition process system for waste remediation, comprising heating the waste in a first chamber to remove moisture, collecting the moisture in a first tank, transferring the moisture from the moisture tank to a waste water filtration system, delivering the heated moisture-free waste from the first chamber to a second chamber, heating the moisture-free waste in the second chamber to produce syngas, transferring the syngas to a second tank, delivering the remaining waste from the second chamber to a third chamber, and heating the remaining waste in the third chamber to produce syngas and char. The system harnesses useable producer gas and converts organic and inorganic waste into bio-char.
Description
where the moisture removal takes place. The burners (56) heat the first chamber (17) ~ with temperatures between 175 — 300 °C. As the waste continuous to travel, it reaches - the inter-connection drop pipe (18) where the waste goes to the second chamber (19) > where the “cracking” of the waste takes place. The waste is introduced to a much higher ~ temperature, between 300 — 650 °C, to crack and harness the syngas. As the waste ~ continuous to travel to the end of the second chamber (19) to the drop pipe (20), it rt transitions to the “charring stage” and the final harnessing of any residual syngas. In this stage, the waste is subjected to extremely high temperature (650 — 1200°C). The charred I waste goes out of the third chamber (21) through transfer auger (23) to the sealed = biochar collector bin (25) where it is to be cooled down before use. -
Although particular embodiments of the present invention have been illustrated and described, it will be apparent to those skilled in the art that various changes and modifications can be made without departing from the spirit of the present invention. it is therefore intended to encompass within the appended claims all such changes and modifications that fall within the scope of the present invention.
Cs 5)
MULTI-STAGE WASTE REMEDIATION SYSTEM o - 7 "
TECHNICAL FIELD oo 4 ol & od
The present invention relates to waste remediation pfocesses, in particular to a self- ro sustained multi-stage thermal decomposition procesysystem for waste remediation. The " system harnesses useable producer gas (syngas) fr 1 solid wastes and converts organic . and inorganic waste into bio-char. ©
Solid wastes are usually disposed by burying them into landfills, burning in incinerators or through recycling. In highly urbanized areas, the biggest challenge is to come up with an effective and environment friendly solid waste and pollution control strategies. One such strategy is pyrolysis, or the decomposition of waste through high temperatures. The current pyrolysis technology only offers two stages in their processes. To achieve an almost 100% waste free solution to the waste problem, the present invention offers a multi-stage thermal decomposition processes embedded within the system; a built-in wastewater treatment; plus, the ability to produce oxyhydrogen through HHO generator system, which makes the present invention a viable, efficient, and effective solution to the waste problem. oT
The present invention is to be used in remediating waste problems. The reclamation of contaminated landfills back into useful land that is free of harmful contaminants, the eradication of derived diseases from landfill leachates and the creation of energy and bio- char from waste are some of the advantages of this invention.
The difference of the present invention from the existing technologies are the embedded multi-stage thermal decomposition process which could set multiple temperature ranges atdifferent stages of the process simultaneously; and the inclusion of a moisture removal stage and the water treatment stage together with the oxyhydrogen production capability, which optimizes the effectiveness and efficiency of the system in remediating ~ almost the entire waste problem. - i"
The present invention overcomes the environmental and health issues directly and = indirectly derived from the landfills and its surrounding. ’ .
The present invention is a waste remediation system comprising heating the waste in a = first chamber to remove moisture, collecting the moisture in a first tank, transferring the ~ moisture from the moisture tank to a waste water filtration system, delivering the heated moisture-free waste from the first chamber to a second chamber, heating the moisture- free waste in the second chamber to produce syngas, transferring the syngas to a second tank, delivering the remaining waste from the second chamber to a third chamber, and heating the remaining waste in the third chamber to produce syngas and char.
The pyrolyzed organic and inorganic wastes are heated at temperatures preferably between 175-300°C in the first chamber to yield moisture, continued heating at temperatures preferably between 300-650°C in the second chamber to produce syngas, and further heating at temperatures preferably between 650-1200°C in the third chamber to produce bio-char and the final harnessing of any residual producer gas (syngas).
The waste remediation method may further comprise the step of collecting the syngas produced in the second and third tanks and separating the gas from liquid by reflux to produce fuel.
The method further may comprise the step of producing oxyhydrogen “HHO” from the moisture by electrolysis to augment syngas production. The oxyhydrogen from the moisture is piped for point of use as fuel augmentation for the system and for the electric generator. The syngas is then collected in a reflux tank for its main usage as fuel for the system and in the electric generator as well.
RR
Preferably, the multi-stage waste remediation system of the present invention ® comprises: a hopper to initially hold the waste; a plurality of chambers for pyrolyzing the ~ waste; a means by which to transport the waste from the hopper to the chambers; a = heating element for each chamber to heat the waste transported to the chamber; a first tank to contain gaseous substances released from the heating of waste in the first " chamber; and a second tank to contain gaseous substances released from the heating of waste in the second chamber. oo
Furthermore, according to the present invention, the first tank is connected to a - wastewater filtration system which is also connected to the oxyhydrogen (HHO) generator system and the second tank is connected to a reflux tank.
These and other underlying purposes and advantages of the present invention will be fully understood upon a perusal of the following detailed description.
FIGURE 1 is a process flow diagram of the present invention;
FIGURE 2 is the perspective view of the present invention;
FIGURE 3 is a sectional view showing the details of the chamber;
FIGURE 3A is a partial view of the end chamber of FIGURE 3; and
FIGURE 4 is a process flow diagram of the first, second and third chambers.
The solid wastes are brought to the facility for segregation. In the segregation process, the organic and inorganic wastes are separated from cement, glass, and metals. The separated cement, glass and metals are brought to a recycling plant, while the organic and inorganic materials are shredded before being subjected into the system as waste.
in the present invention, the burners in the chambers are pre-heated to the desired = temperature prior to the introduction of the waste to the system. Waste is initially ol contained in the hopper and the transfer auger moves the waste from the hopper to the first chamber after pre-heating. The main motor starts to turn and drive the gears connected to the chamber’s augers at a selected speed through a chain drive. o
The auger inside the first chamber turns to push the waste along the walls of the heated . chamber (175 — 300 °C) where the moisture removal stage takes place. The removed - moisture goes to the moisture collection tank then to the built-in wastewater treatment © system before disposal for irrigation. A small percentage of the treated wastewater goes @ to the HHO system for hydrogen production to augment the producer gas (syngas) in powering the system and the generator.
As the waste continuous to travel, it reaches the inter-connection drop pipe where the waste goes to the second chamber where the “cracking” of the waste takes place. The waste is introduced to a much higher temperature (300 — 650 °C) to crack and harness the syngas. The syngas travels through pipes and then contained in the second and third tanks where the gas is separated from the liquid by reflux and produces fuel for the system. The remaining syngas will fuel the electric generator.
As the waste continuous to travel to the end of the second chamber to the drop pipe, it transitions to the “charring stage” and the final harnessing of any residual syngas. In this stage, the waste is subjected to extremely high temperature (650 — 1200°C). The charred waste goes out of the third chamber through transfer auger to the sealed biochar collector bin where it is to be cooled down before use.
The present invention will be more particularly described hereunder with reference to
FIGURES 1 to 4.
FIGURE 1 is a structure diagram and FIGURE 2 is an isometric view of the multi-stage waste remediation system.
oe
As shown in FIGURES 1 and 2, the multi-stage waste treatment system (10) comprises a = supply unit hopper (13) and a transfer auger (15) for supplying the waste containing = organic substance into the system (10) and thermal decomposition units for pyrolyzing nN the wastes. The thermal decomposition unit comprises three chambers: first (17), second =o (19) and third (21), for drying, cracking and charring the wastes respectively. - o
The first chamber (17) is connected to the supply unit (13) for removing moisture at the ” initial stage. The second chamber (19), where cracking takes place, is connected to the ~ first chamber (17) and a third chamber (21), where the wastes are further decomposed © to become char, is connected to the second chamber (19). The third chamber (21) is then © connected to a transfer auger (23), which in turn is connected to a biochar bin (25) for collecting and storing the charred wastes.
A drive motor (51) is used for driving a gear system (53) for transferring the waste from the first chamber (17) to the second chamber (19) and to the third chamber (21) and then the charred wastes from the third chamber (21) to the transfer auger (23) and to the final biochar bin (25).
A control panel (11) connecting to the system is used for controlling the desired temperatures of each chambers. The reflux tank (35) is connected to the burners (56) through a gas pipe assembly (55) where the mixture of HHO and syngas are being used for heating the chambers.
Pipes (26) from the first chamber (17) are connected to a first tank (27) for collecting moisture. The multi-stage waste treatment system (10) has a built-in waste water filtration system (41) and a hydrogen/oxygen (HHO) system containing: an HHO water reservoir (43), an HHO generator (45), an HHO water pump (47) and an HHO cooling system (49), which are initially connected to the first tank (27). The moisture collected from the first tank (27) is treated in the water filtration system (41) before disposal and a portion of the treated wastewater goes to the HHO water reservoir (43) through a pipe (42) for producing hydrogen to supply the producer gas in powering the HHO system and generator.
Pipes (28) from the second chamber (19) and third chamber (21) are connected to the o second tank (29) and further connected to the third tank (31) to produce syngas by os gasification. Syngas is then collected to the second tank (29) and further condensed to = separate gas from liquid in order to remove impurities. The condensed gas from the - second tank (29) are transferred to the third tank (31) through a pipe (30) for further ~ condensing. The pipe (32) on top of the third tank (31) is connected to a reflux pump (33) " and into the reflux tank (35) for transferring the purified syngas. ~
A compressor (37) connecting from the reflux tank (35) through a pipe (40) is used for - compressing the excess fuel. The compressed fuel is transferred to and stored in a storage tank (39) through a pipe (38) for further use or consumption.
A small amount of the oxyhydrogen produced from the HHO system is also transferred to the valves (36) through a pipe (34). The purified syngas from the storage tank (39) and oxyhydrogen from the HHO system are combined through proper mixing ratio. The mixture is used as fuel to run the electric generator (not shown) and as fuel for the burners (56) to run the entire multi-stage waste treatment system (10).
FIGURE 3 is a sectional view showing the structure of the chamber. An enlarged detail of the end portion of the said chamber is shown in FIGURE 3A. Inside the chamber housing (59) is a series of metal plates/auger (61) connected to the shaft (62) for pushing the waste along the walls of the chamber. A shaft sleeve (63) is connected to the chamber housing (59) to hold the auger (61) in place. A spur gear (65) is connected at the end of theshaft sleeve (63) as a locking mechanism. At the opposite side of the chamber housing (59) is a shaft sleeve (63) where the gear mechanism is located. As shown in Figure 3A, the gear mechanism contains a shaft seal (67) and a shaft bearing (69). The end of the shaft contains a bolt (73) and a pin (75) which are connected to the gear hub (71) to prevent lateral movement.
Flow details of this process is also shown in FIGURE 4, wherein the auger (77) inside the first chamber (17) turns to push the waste along the walls of the heated chamber (17)
Claims (11)
1. A method for treating waste comprising: ol - heating the waste in a first chamber to remgve moisture; i - collecting the moisture in a first tank; - - transferring the moisture from the isture tank to a waste water i filtration system; = - delivering the heated moisture-free waste from the first chamber to a second chamber; He - heating the moisture-free waste in the second chamber to produce syngas; - transferring the syngas to a second tank; - delivering the remaining waste from the second chamber to a third chamber; and - heating the remaining waste in the third chamber to produce syngas and char.
2. The method according to claim 1, further comprising the step of collecting the syngas produced in the second and third tanks and separating the gas from liquid by reflux to produce fuel.
3. The method according to claim 1 wherein the heating temperature in the first chamber is between 175-300°C.
4. The method according to claim 1 wherein the heating temperature in the second chamber is between 300-650°C.
5. The method according to claim 1 wherein the heating temperature in the third chamber is between 650-1200°C.
6. The method according to claim 1, further comprising the step of producing - oxyhydrogen “HHO” from the moisture by electrolysis to augment syngas production. "
-
7. The method according to claim 6 wherein the oxyhydrogen and syngas are - contained in a reflux tank for use as fuel -
8. A multi-stage waste treatment system comprising: ~ - a hopper to initially hold the waste; © - afirst chamber; - asecond chamber; - athird chamber; - means by which to transport the waste from the hopper to the chambers; - a heating element for each chamber to heat the waste transported to the chamber; - a first tank to contain gaseous substances released from the heating of waste in the first chamber; and - asecond tank to contain gaseous substances released from the heating of waste in the second chamber.
9. The waste treatment system of claim 8, wherein the first tank is connected to a wastewater filtration system.
10. The waste treatment system of claim 8, wherein the second tank is connected to a reflux tank.
11. The waste treatment of claim 10, wherein an oxyhydrogen (HHO) generator system is piped for point of use as fuel augmentation for the system
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PH12017000201A PH12017000201A1 (en) | 2017-07-11 | 2017-07-11 | Multi-stage waste remediation system |
| PCT/PH2018/000011 WO2019013655A2 (en) | 2017-07-11 | 2018-07-10 | Multi-stage waste remediation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PH12017000201A PH12017000201A1 (en) | 2017-07-11 | 2017-07-11 | Multi-stage waste remediation system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| PH12017000201A1 true PH12017000201A1 (en) | 2019-02-11 |
Family
ID=63998730
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PH12017000201A PH12017000201A1 (en) | 2017-07-11 | 2017-07-11 | Multi-stage waste remediation system |
Country Status (2)
| Country | Link |
|---|---|
| PH (1) | PH12017000201A1 (en) |
| WO (1) | WO2019013655A2 (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3020212A (en) * | 1959-11-04 | 1962-02-06 | Pan American Resources Inc | Refuse converter |
| US20070244208A1 (en) * | 2006-03-20 | 2007-10-18 | Shulenberger Arthur M | Process for producing liquid fuel from carbon dioxide and water |
| US20160146105A1 (en) * | 2014-11-21 | 2016-05-26 | Kevin Phan | Method and Device for Converting Municipal Waste Into Energy |
| US9657989B2 (en) * | 2008-04-07 | 2017-05-23 | Wastedry, Llc | Systems and methods for processing municipal wastewater treatment sewage sludge |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2325288A1 (en) * | 2009-11-20 | 2011-05-25 | RV Lizenz AG | Method and device for thermal-chemical processing and exploitation of substances containing carbon |
| GB2539447B (en) * | 2015-06-16 | 2017-07-05 | Sage & Time Llp | Converting a carbonaceous feedstock into a product gas e.g. methane gas |
-
2017
- 2017-07-11 PH PH12017000201A patent/PH12017000201A1/en unknown
-
2018
- 2018-07-10 WO PCT/PH2018/000011 patent/WO2019013655A2/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3020212A (en) * | 1959-11-04 | 1962-02-06 | Pan American Resources Inc | Refuse converter |
| US20070244208A1 (en) * | 2006-03-20 | 2007-10-18 | Shulenberger Arthur M | Process for producing liquid fuel from carbon dioxide and water |
| US9657989B2 (en) * | 2008-04-07 | 2017-05-23 | Wastedry, Llc | Systems and methods for processing municipal wastewater treatment sewage sludge |
| US20160146105A1 (en) * | 2014-11-21 | 2016-05-26 | Kevin Phan | Method and Device for Converting Municipal Waste Into Energy |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2019013655A3 (en) | 2019-02-21 |
| WO2019013655A2 (en) | 2019-01-17 |
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