Method of utilization of refuse and device for executing the said method
11 claims: 4 independent, 7 dependent
- 1Způsob zužitkování odpadků, podle něhož se rozdrcené odpadky z domácnosti, průmyslové odpadky a jiné speciální odpadky směšují s vodou, rozdělí se na organické a anorganické složky, proud odpadní vody se spolu se složkami odpadků, které jsou v něm rozpuštěny a suspendovány, nejprve filtruje neaktivovaným a poté aktivovaným uhlím, tuhé odpadky, popřípadě část filtračního uhlí nasyceného nečistotami se spálí, další část filtračního uhlí nasyceného nečistotami se tepelně zpracovává při teplotě 300 až 800 °C a regeneruje a regenerované filtrační uhlí se popřípadě po jeho aktivaci zavádí zpět do oblasti filtrace odpadní vody, vyznačující se tím, že při nízkotepelném spalování se přivádí kyslík v podstechiometrickém množství, filtrační uhlí nasycené nečistotami se v tepelném rozkladném procesu v prostředí prostém kyslíku odplyňuje a nečistoty uipělé na filtračním uhlí se při 300 až 800 °C rozkládají, regenerované uhlí nebo jeho část se sbaluje, vzniklé topné, popřípadě nízkotepelným spalováním vzniklé plyny, nebo jejich část, se po využití tepla obsaženého v plynu v pásmu s vysokou teplotou nejméně 1300 °C při dokonalém vyloučení kyslíku krakují, plyny vystupující z pásma s vysokou teplotou se chladí a zkapalňují, přičemž se kapalný dusík odděluje od kapalného topného plynu prostého dusíku a odpadní plyn, odváděný do atmosféry, se filtruje přes uhlí.
- 2Způsob podle bodu 1, vyznačující se tím, že teplota při nízkotepelném spalování dosahuje nejvýše 800 °C.
- 3Způsob podle bodů 1, 2, vyznačující se tím, že teplem, které se uvolňuje při nízkotepelném spalování se ohřívá filtrační uhlí nasycené nečistotami.
- 4Způsob podle bodů 1 až 3, vyznačující se tím, že se tuhé odpadky spalují při teplotě 500 až 800 °C.
- 5Způsob podle bodů 1 až 4, vyznačující se tím, že objem přivedeného kyslíku činí v závislosti na složení a obsahu vlhkostí tuhých odpaků 30 až 90 %' stechiometrú* ky potřebného množství vzduchu. VYNALEZU
- 6Způsob podle bodů 1 až 6, vyznačující se tím, že se uhelný prach, obsažený v regenerovaném uhlí, odlučuje a zpracovává na uhelné sbalky.
- 7Způsob podle bodu 1, vyznačující se tím, že se vyrobené, popřípadě regenerované uhlí po předběžném zpracování aktivuje a popřípadě sbaluje.
- 8Způsob podle bodu 7, vyznačující se tím, že se tepelným rozkladným procesem nově získané, popřípadě regenerované, filtrační uhlí před aktivací jemně rozemele a smísí se v poměru 10 :1 až 5 : 1 s pojivém jako dehtem nebo smolou, získaná směs se pod vysokým tlakem zvláště 100 až 200 MPa, a při dostatečném změknutí pojivá jako dehtu nebo smoly utváří do kompaktní formy, načež se rozemele.
- 9Způsob podle bodu 1, vyznačující se . tím, že teplem, získaným z odpadních plynů při nízkotepelném spalování, popřípadě v tepelném rozkladném procesu, se tuhé odpadky a/nebo filtrační uhlí nasycené nečistotami předběžně suší.
- 10Způsob podle bodu 9, vyznačující se tím, že se teplem, získaným z odpadních plynů, ohřívá voda к proplachování aktivního uhlí nasyceného nečistotami.
- 11Zařízení к provedení způsobu podle bodu 1, obsahující přívod odpadní vody a sedimentační nádrž, v níž jsou obsaženy prvky pro hrubou a jemnou filtraci uhlím, popřípadě aktivním uhlím, drtiče odpadků, vícereaktorovou pec s alespoň jedním reaktorem pro tepelný rozklad umístěným v horní části vícereaktorové pece, a s alespoň jedním reaktorem pro rozklad spalováním umístěným v dolní části vícereaktorové pece, přičemž uvedené části jsou umístěny vedle sebe, a obsahující dále ústrojí pro předběžné sušení odpadků, popřípadě filtračního uhlí, vyznačující se tím, že obsahuje sbalovací ústrojí (292) pro spalování vystupujícího uhlí, umístěné za reaktorem (186) pro tepelný rozklad, a mlecí ústrojí (295), jakož i krakovací ústrojí (192) pro štěpení vyšších uhlovodíků obsažených v topném plynu, popřípadě v plynu vzniklém nízkotepelným spalováním.
Independent claims11
41 paragraphs, as filed
The invention relates to a process for the recovery of garbage according to which the crushed household garbage, industrial garbage and other special garbage are mixed with water, separated. to organic and inorganic components, the waste water stream, together with the waste components dissolved and suspended therein, is first filtered by an inactivated and then activated activated carbon, solid waste, or a part of the filter coal saturated with impurities is burned, another part of the filter coal saturated the impurities are thermally treated at a temperature of 300 to 800 ° C and regenerated and the regenerated filter coal is optionally after; it activates it back into the filtration area: waste water. The invention further relates to an apparatus for carrying out said method.
A method of utilizing garbage according to; wherein the waste water serves as; means for transporting waste, the waste is divided into organic and inorganic components and the waste water containing the waste is cleaned by mechanical and adsorption filtration with normal and activated carbon. Thereafter, some of the refuse or activated charcoal with the impurities is incinerated, providing outside the fuel gas the heat required for thermal decomposition. The major part of the filter coal with impurities is thermally decomposed and the filter coal is regenerated to obtain new coal as well as a low-temperature gas.
This method can be improved for optimum energy use. In addition, it is necessary to eliminate the difficulties and disadvantages associated with its implementation. The use of charcoal or activated charcoal produced according to the process results in its abrasion, which results. to the loss of coal, clogging of the filter towers, as well as 1 to the pollution of the process water that is being cleaned.
SUMMARY OF THE INVENTION It is an object of the present invention to improve the energy balance of the improved process by making optimum use of all energy sources, and to ensure a smooth process, which is to be achieved by a particularly streamlined selection of reaction conditions taking place in a multi-reactor furnace.
The principle of the process according to the invention consists in the fact that in low-temperature combustion, oxygen is supplied in a substantially stoichiometric amount. the decomposition process in an oxygen-free environment is degassed and the impurities adhering to the filter coal are decomposed at 300 to 800 degrees Celsius, the recovered coal or a part of it is packaged, gas in the high temperature zone of at least 1300 ° C, with complete exclusion of oxygen, cracking, the gases exiting the high temperature zone are cooled and liquefied, wherein the liquid nitrogen is separated from the nitrogen-free liquid fuel gas and the off-gas discharged to the atmosphere is filtered through a coal filter. It is preferred that the temperature in the low-temperature combustion reaches a maximum of 800 ° C. The heat released by the low-temperature combustion heats the filter coal saturated with impurities. Solid waste is burned at 500 to 800 ° C. Depending on the composition and moisture content of the solid debris, the amount of oxygen introduced amounts to 30 to 90% of the stoichiometrically required amount of air. The coal dust contained in the recovered coal is separated and processed into coal pellets. The produced or regenerated coal is activated or packaged after pretreatment. The filter charcoal obtained by the thermal decomposition process is finely ground and activated in a ratio of 10: 1 to 5: 1 with a binder such as tar or pitch, before being activated, the mixture obtained under high pressures, in particular 100 to 200 MPa, and when sufficiently softened, the binder of tar or pitch forms into a compact mold and is then ground. The solid waste and / or impregnated filter coal is pre-dried by the heat obtained from the off-gases in the low-temperature combustion or in the thermal decomposition process. The heat obtained from the waste gases heats the water to flush the activated carbon saturated with impurities.
The known waste utilization device comprises a waste water inlet and a sedimentation tank containing elements for coarse and fine filtration with charcoal or activated charcoal, a waste shredder, a multi-reactor furnace with at least one reactor for thermal decomposition located in the upper part of the multi-reactor furnace. one combustion decomposition reactor located in. the lower parts of the multi-reactor furnace, said parts being placed side by side and further comprising a means for pre-drying the refuse or filter coal. The apparatus according to the invention consists of a packer for the combustion of the exiting coal, downstream of the thermal decomposition reactor, and a grinding means, as well as a cracker for the cracking of the higher hydrocarbons contained in the fuel gas or gas produced by low-temperature combustion.
An advantage of the process according to the invention is a particularly advantageous combination of the various process steps allowing maximum utilization of the energy of the processes taking place in a multi-reactor furnace, the heat production during pyrolysis or combustion being controlled by dosed oxygen supply and the remaining energy being obtained in a relatively high content hydrocarbon. By means of the method according to the invention, depending on the composition of the garbage, it is possible to keep the garbage recovery plant in operation without supplying external energy and in addition to obtaining additional energy.
Under the particularly favorable conditions selected in the multi-reactor furnace, filter coal with good adsorption properties as well as a low-temperature gas of particularly highly enriched hydrocarbons are obtained during thermal decomposition. By special treatment of the heating and / or low-temperature gases exiting the multi-reactor furnace, accumulative energy is obtained, the heat of the gases being utilized by means of a heat exchanger in a device according to the invention for pre-drying, reheating water or for thermal decomposition. In addition, the difficulty of carrying out the process by specifically treating the filter coal exiting the multi-reactor furnace is eliminated. According to the invention, the recovered coal used in the coarse filter is either packaged, forming a 'compact shape with the desired particle size, thereby eliminating the abrasion of the coal and the resulting re-contamination of purified water as well as clogging of filter elements filled with filter coal. or, by pretreating the coal in the fine filter to be activated, a filter material having a particularly large surface area and thus a high adsorption capacity is produced.
The individual steps of the process according to the invention will be explained in more detail below.
The temperature during low-temperature combustion should not exceed 800 ° C. A particularly preferred range of this temperature is between 500 and 800 ° C. In case of danger of evaporation of certain heavy metals the temperature is maintained. with low-temperature combustion in the range of 300 to 400 ° C. In low-temperature combustion, oxygen is supplied in a substantially stoichiometric amount to conduct the pyrolytic process, but the temperature does not rise above 800 ° C. The amount of oxygen supplied is about 30 to 90% of the stoichiometrically required amount, preferably 50 to 80%. The specific amount of oxygen supplied depends on the composition of the combusted charge and the degree of its moisture content.
The resulting heating or low-temperature gas can be used as an additional external energy source for thermal decomposition or as a fuel for a separate boiler, gas-firing device, in particular a combustion machine or the like.
In addition, it is possible to treat the heating or low-temperature gas in the cracker to break down the higher hydrocarbons into lower hydrocarbons, which can be used directly in combustion machines, turbines and the like, or which, after liquefaction, provide an easily storable energy source.
In the process according to the invention, it is preferable to o215012
6 cooling the gases exiting the high temperature region to a sufficient extent to liquefy them, optionally separating liquid nitrogen and a liquid flammable, nitrogen-free gas such as methane.
At a temperature of at least 1300 ° C, higher hydrocarbons are split into lower hydrocarbons in the oxygen-poor high temperature range. The cracking of the higher hydrocarbons can also be carried out with the exclusion of oxygen, so that combustion or oxidation of the gas obtained does not occur.
The coal dust contained in the recovered coal is separated and processed to obtain sufficient hardness and, as far as possible, uniform particle size. coal packs.
After pre-treatment, the produced or regenerated coal is activated and optionally packed. To this end, the filter coal newly obtained or regenerated is finely ground and mixed in a ratio of 10 1 to 5: 1 with a binder such as tar or pitch; under high pressures, in particular 100 to 200 MPa, and with sufficient softening, the binder is formed into a compact mold and then ground on either a rolling mill or hammer crushers. When grinding, it is important to keep the dust content at a low level.
The particle size to which the filter coal is milled depends on the intended use. A suitable activated carbon used to purify liquids has a particle size of between 0.5 and 1.5 mm. The activated carbon used to purify the gas preferably has a particle size of between 2 and 3 mm.
The fragmentary granulate or briquettes of the desired size can be activated in the activator according to a conventional method by superheated steam or chemicals. Activated carbon having a particularly high adsorption capacity is obtained. The activated carbon is preferably packed in a packaging device.
The method and apparatus of the invention are described in detail in the following description and illustrated by way of example, but not limited to the accompanying drawings, in which: Fig. 1 is a schematic diagram of a garbage recovery method according to the invention; Figs. 2a and 2b 3 shows a schematic diagram for the production, use and regeneration of normal and active filter coal according to the invention, FIG. 4 is a vertical section. FIG. 5 4 shows a vertical section along line 5--5 in FIG. 4 by a multi-reactor furnace; and FIG. 6 shows a schematic cross-section through a cracker.
Giant. 1 illustrates in a schematic diagram the material flow during solid and liquid waste treatment in the waste recovery and waste water treatment plant 102 of the invention. The apparatus 102 comprises a multi-reactor furnace 104. Solid wastes for processing, which may include, but are not limited to, food waste, paper, plastic, oil and tar residues, old tires, wood, glass, ash and the like, are pre-treated by magnetic strip separation, pulping and waste water flotation in such a way that they become essentially organic components for further processing. In the multi-reactor furnace 104, the solid refuse is combusted, decomposed by combustion in the first reactor in an oxygen-poor environment to produce heat, fuel gas and ash.
Waste water, which can be both urban waste water and industrial waste water, is passed through a multi-stage coal filter 106 for waste water treatment, so that it can be utilized at least for industrial purposes. The coal filter 106 is preferably a two-stage filter consisting of a coarse filter 114 and a fine filter. 116. The coarse filter charcoal is regenerated together with the particles adhering to the coal and with the mud periodically in the multi-reactor furnace 104, that is, subjected to heat treatment in the absence of oxygen. Newly recovered and recovered coal compensates for coal losses.
Giant. Figures 2a and 2b, supplemented with Figure 3, show an overview of the process in the waste recovery plant 102, and waste water is also treated, since the waste water inlet channel 108 leads wastewater through the sedimentation tank 110 and the screen 112 first to the coarse filter 114 and then to the fine filter 116 from where it continues through the discharge channel 11fiL
The coarse filter 114 consists of a set of coarse filter elements 120 that can leave the coarse filter by raising and lowering for regeneration, or can be reintroduced. Each coarse filter element 120 is filled with normal filter coal of a suitable particle size, preferably packed filter coal.
The coarse filter elements 120, in operation, move countercurrent to the wastewater flow from the end portion 122 of the coarse filter 114 to the initial portion 124 of the coarse filter 114.
The fine filter 116 consists of another set of fine filter elements 126 of the fine filter 116, which also move in countercurrent to the waste water from the end portion 128 of the fine filter 116 to the initial part 130 of the fine filter 116. The fine filter 116 can be backwashed, optionally in the backwash devices 134. Preferably, the backwash water is taken directly from the outlet channel 118, and may be stored for a period of time in a container 136 equipped with heating coils 138. By backwashing, the contaminated water flows through the return line 140 back to the waste water inlet channel 108. For processing, solid debris is placed in a container 160 where on a magnetic belt 162, a conveyor 166
215 12 and between the crushing rollers 164 there is a first treatment - disintegration of the garbage. In the sedimentation tank 110, substances with a density> 1 are separated and removed by means of a bucket conveyor 168. A series of air nozzles 170 ensure a perfect mixing of waste water and garbage, facilitating their separation into organic and inorganic components. The discharge conveyor 132 transports the flotation organic matter to a pair of storage chambers 172 of the multi-reactor furnace 104. In addition, further garbage may be fed continuously to the storage chambers 172 through conveyor belts 174.
A multi-reactor furnace 104 in which combustion and decomposition of garbage and / or filter coal with impurities occurs simultaneously in different reactors is shown in FIGS. 4 and 5. A pair of reactors 178 serves to incinerate or pyrolize the garbage and / or filter coal with dirt. In another reactor 186 thermal decomposition of the saturated filter coal or waste material occurs.
The interior 190 of the multi-reactor furnace 104 is bounded by a sheath 222. The shafts 224 of the reactors 178 and 18a are housed in bearings 226 and are driven by a drive mechanism 228, for example an electric motor 230. All reactors 178 and 186 are filled and emptied. 236 with a device for closing them. Double-leaf doors 234, 236 are provided with hinges 262. In addition, the reactor pair 178 is provided with an air supply line 238, a fuel gas outlet 240, and convex sieves 242. The reactor pair 178 is additionally connected to a gas line 184 provided with a check valve 246 and flowing into the cracker 192 followed by a scrubber 196. A gas line 184 is provided with a branching line 248 with a valve 250.
The garbage collector 252 is provided with a bottom plate 254 in the bottom part which separates the collecting space 256 arranged below. In the lower part of the collecting space 256 there is a support plate 258 with thermal insulation 260 which is provided with a joint (not shown).
Also, another down-opening collecting space 264 is provided with a further plate 286 provided with a hinge (not shown). After thermal decomposition or combustion decomposition, the solids from the reactors 178 and 186 are discharged into funnel tanks 268 and 270, which are provided with exchanger coils 272 on the surface and a slide 274 at the bottom.
In addition, air can be supplied to the interior 190 of the multi-reactor furnace
104 supply line 278 with valve 280.
Above the thermal decomposition reactor 186 there is a gas discharge line 282 with a valve 284. In addition, the thermal decomposition reactor 186 is equipped with a heat exchanger 288.
The coal formed in the reactor 186 is screened through a sieve 290 - FIG. 3. Larger coal particles can be used directly in the coarse filter 114. Smaller sized coal particles and coal dust are processed into bales of desired particle size in the packer 292. These packs also serve to fill the coarse filter elements 120 of the coarse filters 114. To produce activated carbon, the filter coal from the reactor 186 is pretreated, i.e., finely ground in a milling device 295, then optionally packed and milled again to the desired grain size. The activation takes place in the activation device 294, which is optionally connected to another packing device 296. The received activated carbon serves to fill the fine filter elements 126 of the fine filter 116 or can be used for commercial purposes.
The above description clearly shows that the waste recovery plant is able to fully produce and regenerate the normal and activated charcoal needed for wastewater treatment.
FIG. 6 shows a cracking device 192 according to the invention in a preferred embodiment. The cracking device 192 consists of a vertical double-walled tank 298 and formed by an outer support tank 304 in which the inner tank 300 is hung behind its upper portion 302. The inner tank 300 has an upper inlet portion 306 covered with an opening lid 308. The lower end of the inner tank 300 has a constriction 310 with a screen 312. Below it is in the outer support tank 304 another screen 316.
The constriction 310 is surrounded by an air supply duct 318. The ring duct 318 is provided with a plurality of air nozzles 320 for introducing combustion air or oxygen into the inner tank 300 through a screen 312. The gas line 184 leads the fission gas to the top of the inner tank 300 and terminates in a funnel opening 322 pointing downward. The inner tank 300 is filled with relatively large particles of combustible material, preferably wood, so that it fills a major part of the interior space between the screen 312 and the funnel opening 322. The wood immediately above the screen 312 is ignited and oxygen is introduced through the air nozzles 320. for burning, so that a high temperature region is formed, but occupies only a relatively small portion above the screen 312, while the remaining combustible material in the inner tank 300 remains relatively cold. After the high temperature region has reached the desired temperature of at least 1300 ° C, fuel gas or low-temperature gas is introduced into the cracking apparatus 192 via gas line 184. In addition, the blower 324 is actuated and a slight negative pressure is generated in the outer support tank 304, causing the gas
Driven by the gas line 184, it draws through the cold region of the combustible material and the high temperature region into the annular space 326 between the outer support tank 304 and the inner tank 300 through the suction line 328 and the blower 324.
The fission gas obtained can either be fed directly to the combustion machine 202 or can be liquefied in a liquefaction plant, optionally separated into methane-based gas and liquid nitrogen.
At periodic intervals, a new combustible material is fed to the cracker 192 with the lid 308 open. This feed can also be carried out continuously.
6 sheets
Sheet 1 Sheet 2 Sheet 3 Sheet 4 Sheet 5 Sheet 6
88 members in 28 offices
Priority claims4
| Document | Office | Kind | Date |
|---|---|---|---|
| 82414877 | United States of America | A | |
| 82414877 | United States of America | A | |
| 77824148 | – | – | – |
| US19770824148 | – | – | – |
Members88
| Document | Office | Kind | |
|---|---|---|---|
| DE2558703A1 | Germany | A1 | |
| DE2602306A1 | Germany | A1 | |
| DE2606451A1 | Germany | A1 | |
| DE2606452A1 | Germany | A1 | |
| PT68416A | Portugal | A | |
| PT68417A | Portugal | A | |
| BE869693A | Belgium | A | |
| BE869694A | Belgium | A | |
| DK350578A | Denmark | A | |
| DK350578A | Denmark | A | |
| DK350678A | Denmark | A | |
| DK350678A | Denmark | A | |
| FI782354A | Finland | A | |
| FI782354A | Finland | A | |
| FI782355A | Finland | A | |
| FI782355A | Finland | A | |
| NO782736L | Norway | L | |
| NO782737L | Norway | L | |
| SE7808559L | Sweden | L | |
| SE7808560L | Sweden | L | |
| NL7808434A | Netherlands (Kingdom of the) | A | |
| NL7808434A | Netherlands (Kingdom of the) | A | |
| NL7808435A | Netherlands (Kingdom of the) | A | |
| NL7808435A | Netherlands (Kingdom of the) | A | |
| DE2834717A1 | Germany | A1 | |
| DE2834718A1 | Germany | A1 | |
| GB2002647A | United Kingdom | A | |
| GB2003128A | United Kingdom | A | |
| FR2399857A1 | France | A1 | |
| FR2399859A1 | France | A1 | |
| BR7805183A | Brazil | A | |
| BR7805183A | Brazil | A | |
| BR7805184A | Brazil | A | |
| BR7805184A | Brazil | A | |
| JPS5463462A | Japan | A | |
| JPS5463548A | Japan | A | |
| US4157961A | United States of America | A | |
| PL209010A1 | Poland | A1 | |
| PL209011A1 | Poland | A1 | |
| US4165289A | United States of America | A | |
| ZA784336B | South Africa | B | |
| ZA784337B | South Africa | B | |
| ES472532A1 | Spain | A1 | |
| ES472533A1 | Spain | A1 | |
| DD138883A5 | German Democratic Republic (until 1990) | A5 | |
| DD138884A5 | German Democratic Republic (until 1990) | A5 | |
| AT360445B | Austria | B | |
| AU3880678A | Australia | A | |
| AU3880678A | Australia | A | |
| AU3880778A | Australia | A | |
| AU3880778A | Australia | A | |
| ATA585078A | Austria | A | |
| PL118042B1 | Poland | B1 | |
| PL118046B1 | Poland | B1 | |
| AU520685B2 | Australia | B2 | |
| GB2003128B | United Kingdom | B | |
| CA1124183A | Canada | A | |
| AU522793B2 | Australia | B2 | |
| CS215012B2This record | Czechoslovakia (until 1993) | B2 | |
| HU178995B | Hungary | B | |
| GB2002647B | United Kingdom | B | |
| YU192378A | Yugoslavia, later Serbia and Montenegro (until 2006) | A | |
| HU179678B | Hungary | B | |
| IL55260A | Israel | A | |
| IL55261A | Israel | A | |
| YU192278A | Yugoslavia, later Serbia and Montenegro (until 2006) | A | |
| CH634536A5 | Switzerland | A5 | |
| CA1144082A | Canada | A | |
| ATA585178A | Austria | A | |
| SU1061705A3 | Soviet Union (until 1991) | A3 | |
| AT374774B | Austria | B | |
| MX5769E | Mexico | E | |
| MX5889E | Mexico | E | |
| CH644888A5 | Switzerland | A5 | |
| NO151530B | Norway | B | |
| FR2399857B1 | France | B1 | |
| NO151530C | Norway | C | |
| YU40044B | Yugoslavia, later Serbia and Montenegro (until 2006) | B | |
| IT1108568B | Italy | B | |
| IT7868897A0 | Italy | A0 | |
| IT7868897D0 | Italy | D0 | |
| FR2399859B1 | France | B1 | |
| IT1160588B | Italy | B | |
| IT7868898A0 | Italy | A0 | |
| IT7868898D0 | Italy | D0 | |
| DE2834718C2 | Germany | C2 | |
| DE2834717C2 | Germany | C2 | |
| DE2558703C2 | Germany | C2 |
Numbers
- Publication, DOCDB
- 215012
- Publication, EPODOC
- CS215012
- Application
- 785120
- Application, DOCDB
- 512078
- Application, EPODOC
- CS19780005120
Titles
- English
- METHOD OF UTILIZATION OF REFUSE AND DEVICE FOR EXECUTING THE SAID METHOD
Classification
- CPC, 10
- C02F11/123
- C02F1/283
- C02F9/00
- C02F11/10
- C10B53/00
- C10G1/002
- Y02E20/12
- Y02W10/40
- Y02P20/129
- Y02W10/30
- IPC, 12
- B01D15 00
- B01D33 00
- B01D33 327
- C02F1 28
- C02F9 00
- C02F11 00
- C02F11 10
- C02F11 123
- C05F15 00
- C10B53 00
- C10G1 00
- F23G5 00
