SYNGAS BY SUPERHEATED STEAM.

Field of the Invention

The present invention relates to the field of gasification processes. More particularly, the invention relates to a method and apparatus for superheated steam gasification.

Background of the Invention

Gasification processes typically involve reacting at relatively high temperatures carbonaceous (carbon containing) materials with air, oxygen, and/or steam to produce a syngas. Some types of carbonaceous materials include coal, petroleum, biomass, organic waste, and the like.

The gasification process may be described by the following chemical equation:

or

where C is carbon (a material which may be gasified, gasifiable material) in the carbonaceous material and H2O + heat is steam, and which during a gasification process in a reactor results in carbon monoxide (CO) and hydrogen (H2), both of which are relatively highly combustible and may be used as syngas. In a second gasification stage, by introducing a controlled amount of oxygen into the reactor foUowing the first gasification stage, the above chemical equation may be transformed as follow- ^'

CO + H2+ O2 from air » CO2 + H2O + heat or C02 + 2H2 + 202 from air » C02 + 2H20 + heat so that what essentially is left after the second gasification stage is carbon dioxide (CO2) and steam (H2O + heat), both of which are non-polluting and non-toxic and may be released into the environment. Generally, following the first or the second gasification stage, what is left of the carbonaceous material is usually in the form of ash, slag, and the like.

U.S. Patent Publication No. 2008/0034658 Al to Reiser et al. relates to "A method and device which enables an oxygen- free gasification process of both a hydrocarbon-containing (initiation/catalyzing) gas in combination either/both carbonaceous and non-carbonaceous solids and/or liquids or mixture thereof (feedstock material). This is a closed-loop system thus eliminating emissions and preventing environmentally damaging pollution. In one embodiment, a solid feedstock material is utilized, although solids, liquids or slurry may be used. Pulverized solid feedstock martial is first cleansed, dried and then saturated with a hydrocarbon containing gas to displace and remove any air or oxygen from voids in particulate matter. (Liquid feedstock material does not first need to be dried or saturated). The initiation gas is first injected into a high-temperature gasification tube. Simultaneously, gas saturated feedstock material is injected into a feedstock injection tube which openly terminates inside the gasification tube. Extreme heat within the tube (provided by internal electric elements) first begins to rapidly expand the initiating gas. As the initiating gas is reaching maximum expansion and velocity, the feedstock material, which is also heated and expanding, exits the feedstock injection tube and enters into the gasification tube. At this point two things happen simultaneously, heat causes the molecular structure of the initiating gas to dissociate while the feedstock material begins expansion and begins to collide with the dissociated mass from the initiating gas. The cracking of the hydrocarbon chains within the initiating gas causes the release of bond energy and generates great acceleration. The released bond energy, along with the addition of the external energy, rapidly expands the gas and causes the velocity of the moving mixture to rise sharply as it proceeds down the tube. Ultimately the molecular structure of the feedstock material is also dissociated or "cracked" releasing additional bond energy and causing additional heat and acceleration. This reaction produces a hydrogen rich synthesis gas which then exits the gasification tube where it may be further processed to remove certain amounts of hydrogen while still retaining the resultant synthesis gas. Additionally, free electrons are generated which may be converted to electricity through the use of an MHD generator. Resultant high temperature hydrogen as well as synthesis gas is cleansed by a filter and then cooled by liquid cooling jackets where heat is extracted by a circulating liquid. This heated circulating liquid may be directed into an external steam turbine for the further production of electricity. Resultant synthesis gas may be further utilized in external energy, petrochemical or manufacturing processes. Resultant Hydrogen gas may be further utilized for the production of electricity or chemical processes. Since this system takes necessary steps to remove air, oxygen and moisture from feedstock materials as well as not utilizing steam, air, oxygen or combustion in the process, oxidized formations of carbon, sulfur and nitrogen are eliminated or severely restricted."

U.S. Patent No. 4,426,810 to Rudolph et al. relates to "Coarse-grained solid fuels in particle sizes of at least 2 mm are gasified under a pressure of 5 to 150 bars in a fixed bed which is slowly descending and into which the gasifying agents are introduced from below whereas the incombustible mineral constituents are withdrawn as solid ash or liquid slag from the lower end of the bed. Fine-grained solid fuels are gasified in a fluidized bed under a pressure of 1 to 100 bars. Oxygen, steam and/or carbon dioxide are used as gasifying agents for the gasification in the fixed bed and in the fluidized bed. The product gas from the fiuidized-bed gasifier has a temperature of 700° to 1200° C. and is indirectly cooled with water. The resulting steam is fed as gasifying agent to the fixed-bed gasifier. The product gas from the fixed-bed gasifier can be indirectly cooled to produce steam and at least part of said steam is fed as gasifying agent to the fiuidized-bed gasifier. The steam fed as gasifying agent to the fixed-bed gasifier has a temperature of about 300° to 600° C, preferably of about 400° to 500° C. The steam produced by an indirect heat exchange with the product gas from the fixed-bed gasifier can be superheated by an indirect heat exchange with the product gas from the fiuidized-bed gasifier before said steam is fed as gasifying agent to the fiuidized-bed gasifier." U.S. Patent Publication No. US2011/078951 to Blasiak et al. relates to "A gasifier combines two reactors using externally generated preheated high temperature steam injection into the first reactor, where the heating demand for gasification is supplied by the sensible energy from the steam. The gasifier can produce a medium and higher LCV syngas. The first reactor is a fixed bed gasification section where the coarse feedstock is gasified, and the second reactor is an entrained-bed gasification section where the liquid and fine feedstock is gasified. Solid coarse feedstock is de volatilized in the first fixed bed reactor of the gasifier with high- temperature steam, and subsequently, in the second reactor subjected to a higher temperature sufficient to crack and destroy tars and oils. Activated carbon may be formed as co- product. The gasifier may be used with various solid and liquid feedstocks. The gasifier is capable of gasifying such different feedstocks simultaneously."

U.S. Patent No. 7,229,483 to Lewis relates to "A method for gasifying carbonaceous materials to fuel gases comprises the formation of an ultra-superheated steam (USS) composition substantially containing water vapor, carbon dioxide and highly reactive free radicals thereof, at a temperature of about 2400° F. (1316° C.) to about 5000° F. (2760° C). The USS composition comprising a high temperature clear, colorless flame is contacted with a carbonaceous material for rapid gasification/reforming thereof. The need for significant super-stoichiometric steam addition for temperature control. Methods for controlling a gasification/reforming system to enhance efficiency are described. A USS burner for a fluidized bed gasification/reforming reactor, and methods of construction, are described."

All the apparatus and methods described above have not yet provided satisfactory solutions to the problem of efficiently gasifying carbonaceous and non-carbonaceous materials in a single-stage reactor, the single-stage reactor being significantly less expensive to build and operate compared to multi-stage reactors.

It is an object of the present invention to provide a solution to the above-mentioned and other problems of the prior art.

Other objects and advantages of the invention will become apparent as the description proceeds.

Summary of the Invention

An aspect of an embodiment of the present invention relates to a gasifier (100) for producing a syngas (36) from feedstock material (38), comprising a reactor (110) adapted to produce superheated steam and having a reactor chamber (10) including inlets through which the superheated steam flows to the feedstock material (38); a transport mechanism (8) for transporting the feedstock material (38) through the reactor chamber (10); and a vibration inducing device (31) for imparting a vibratory motion to the feedstock material (38).

In some exemplary embodiments, the feedstock material (38) is a carbonaceous material.

In some exemplary embodiments, the feedstock material (38) is a non-carbonaceous material.

In some exemplary embodiments, the reactor (110) is a single-stage reactor.

In some exemplary embodiments, the superheated steam flow is counter-flow.

In some exemplary embodiments, the heat energy in the superheated steam is conducted through walls (7) of the reactor chamber (110) to the feedstock material (38).

In some exemplary embodiments, the vibration inducing device (31) imparts a vibratory motion to the transport mechanism (8).

In some exemplary embodiments, the vibration inducing device (31) includes a steam pulsator (34).

In some exemplary embodiments, the vibration inducing device (31) includes an ultrasound generator (35). In some exemplary embodiments, a pressure in the reactor chamber (10) is approximately 1 atmosphere absolute.

In some exemplary embodiments, the reactor (110) includes at least one steam flow channel (5A, 5B) for producing the superheated steam.

In some exemplary embodiments, the superheated steam is produced from saturated steam.

In some exemplary embodiments, the reactor (110) includes at least one heating channel (9A, 9B) for heating the steam in the at least one steam flow channel (5A, 5B).

In some exemplary embodiments, the heating by the at least one heating channel (9A, 9B) includes heat transfer by conduction.

In some exemplary embodiments, the gasiRer (100) includes a feedstock size-reducing feed system (l).

The foregoing embodiments of the invention are described and illustrated in conjunction with systems and methods thereof, which are meant to be merely illustrative, and not limiting.

Brief Description of the Drawings Embodiments and features of the present invention are described herein in conjunction with the following drawings^

Figure 1 schematically illustrates a single-stage superheating steam gasifier, according to an embodiment of the present invention _* ' Figure 2 schematically illustrates a side view of a section of the reactor of Figure 1, according to an exemplary embodiment of the invention; and

Figure 3 schematically illustrates a cross-sectional top view of the reactor,

It should be understood that the drawings are not necessarily drawn to scale.

Detailed Description of Preferred Embodiments

An aspect of an embodiment of the present invention relates to a single-stage, gasifier configured for gasifying carbonaceous and non-carbonaceous materials using superheated steam. The gasifier includes an air-less/oxygen- less reactor so that use of air or oxygen during the gasification process is not required, thereby eliminating use of incineration during the process. The non-carbonaceous materials may include any element which is more reducing than hydrogen such as, for example, metals and halides (elements combined with halogen). As the reactor processes both carbonaceous and non-carbonaceous materials, sorting of the material prior to being fed into the reactor is not required. For convenience hereinafter, the carbonaceous material and the non- carbonaceous material may also be referred to as "gasifiable mixture" or "feedstock". In some embodiments, the gasifiable mixture may include any type of dry or wet solid, or slurry, or other materials originating from domestic, industrial, medical, agricultural, or other forms of waste. These may include, for example, dangerous materials such as cyanides or polyurethanes containing dangerous compositions such as dioxins, furanes, PCB, and the like. Other examples are biomass, wood, coal, plastics, refinery bottoms and oil, iron and other reducing metals which may be oxidized (reducers), rubber, magnesium chloride, any metallic halide or salt, among many others.

In some embodiments, the reactor is a counter-flow superheated steam reactor, where the superheated steam flows in a direction opposite (counter-flow) to the direction of flow of the feedstock in a reaction chamber. The superheated steam is applied to the feedstock through inlets distributed along at least a portion of a length of the reactor chamber walls, the inlets adapted to conduct the steam flow in the direction of flow opposing that of the feedstock flow inside the reactor. Optionally, the superheated steam inlets are distributed along a length of the reactor chamber and substantially approximate a point of entry of the feedstock into the reactor chamber. Additionally or alternatively, the superheated steam inlets are distributed along a length of the reactor chamber so that they approximate a point of exit of non-gasiflable material from the reactor. For convenience hereinafter, the point of entry of the reactor chamber may be referred to as "proximal end" and the point of exit as "distal end".

In some exemplary embodiments, the superheated steam entering the reactor chamber through the inlets is at a temperature for maintaining a set point temperature of the feedstock substantially uniform along the length of the reactor chamber at 700° C. Alternatively, the set point temperature of the feedstock is at least 400° C, for example, 500° C, 600° C, 650° C, 750° C, 800° C, 900° C, 1000° C, 1200° C, 1500° C, or greater. Optionally, the set point temperature of the feedstock varies along the length of the reactor chamber, the minimum temperature being at least 400° C and preferably 700° C at the proximal end and increasing towards the distal end, for example, to a temperature necessary for oxidizing the other elements used in the reaction by superheated steam gasification, which may be 1250° C. For example, for carbonaceous material, the temperature would be that for oxidizing the carbon for forming hydrogen and carbon monoxide (1000° K) using superheated steam gasification.

In some exemplary embodiments, the temperature of the superheated steam in the inlets is at least 350° C, for example, 400° C, 500° C, 650° C, 750° C, 800° C, 900° C, 1000° C, 1200° C, 1500° C, or greater. Optionally, the temperature of the superheated steam in the inlets may vary according to the location of the inlets along the length of the reactor chamber. In some embodiments, the pressure of the superheated steam during the gasification process is approximately 1 atmosphere absolute. Alternatively, the pressure of the superheated steam may be greater than 1 atm with the disadvantage that the corrosiveness of the steam increases. Other disadvantages associated with high pressure (greater than 1 atm) superheated steam may include blocking of valves and other components having small inlets through which the steam flows (due to materials in the water in the steam).

In some exemplary embodiments, the gasifying process is assisted by the the use of conduction heating through the walls of the reactor chamber into the flow path of the feedstock. Optionally, the conduction heating is combined with the superheated steam counter-flow heating for substantially reaching the set point temperatures in the feedstock as previously described. In some embodiments, the feedstock contacts the reactor chamber walls for improving conduction heating to the feedstock.

In some exemplary embodiments, a heat transfer coefficient between the superheated steam and the feedstock is in a range from 3 W/m ² K - 30 W/m ² K, for example, 3 W/m ² K - 25 W/m ² K, 3 W/m ² K - 20 W/m ² K, 5 W/m ² K - 25 W/m ² K 5 W/m ² K - 20 W/m ² K, 5 W/m ² K - 15 W/m ² K, 8 W/m ² K - 20 W/m ² K, 8 W/m ² K - 15 W/m ² K 10 W/m ² K - 16 W/m ² K, 20 - 60W/m ² K Optionally, the heat transfer coefficient includes heat transfer by conduction through the reactor walls.

In some exemplary embodiments, the gasifier includes a size reducing mechanism for reducing a size of the feedstock entering into the reactor chamber to a predetermined size range, which may range in some embodiment from less than 1mm to lumps as large as 60 mm, and larger. Optionally, a size of the gasifiable material (e.g. carbon, metal, halide) in the entering feedstock ranges from less than 1 mm up to 25 mm, for example, 1 mm, 2 mm, 3 mm, 5 mm, 6 mm, 8 mm, 10 mm, 13 mm, 16 mm, 18 mm, 20 mm, 22 mm, 24 mm, or sizes in between. The size of the entering feedstock and of the gasifiable material, and the rate at which the feedstock flows through the reactor chamber, influences a physical (geometric) and a thermodynamic design of the reactor, and a design of a transport mechanism transporting the feedstock through the reactor chamber (described further on below). In some exemplary embodiments, the feedstock is transported through the reactor chamber on a transport mechanism from the proximal end to the distal end, while being exposed to the superheated steam gasification. Optionally, a transport rate of the transport mechanism ensures that at the distal end all of the gasifiable material has been dissolved leaving only ash and/or slag from the non- gasifiable materials. Optionally, the transport rate of the feedstock is controllable based on the size of the feedstock for ensuring that the lumps are gradually dissolved by the superheated steam while moving along the reactor, in some embodiments, transport rates may vary from a minimum of 10 kilograms per hour to an average 300 kg/hour to a maximum of 1000 kilograms per hour according to the primary size distribution of the feedstock.

In some exemplary embodiments, the transport mechanism includes a vibration inducing mechanism for imparting a vibratory motion to the transport mechanism for vibrating the feedstock as it travels through the reaction chamber. Vibrating the feedstock moves particles in the feedstock, optionally breaking up lumps in the feedstock, so that a greater surface area of the feedstock material is exposed to the superheated steam (increases heat transfer). Optionally, the vibration increases contact between the material and the heat conducting walls of the reactor chamber, further increasing heat transfer from the wall to the feedstock. In some embodiments, the gasifier may include an ultrasound generator for pulsating the superheated steam causing the feedstock to vibrate due to the pulsations. In some exemplary embodiments, syngas is produced as the feedstock travels through the reaction chamber from the proximal end to the distal end. Optionally, the syngas produced varies in composition depending on the location of the feedstock inside the reaction chamber. For example, in some embodiments, a steam temperature of approximately 400° C and reaction chamber wall temperature of approximately 700° C near the proximal end will dissolve approximately 30% of carbonaceous feedstock into syngas of approximate composition CO+l/202+CH4+guest H2; a steam temperature of approximately 550° C and reaction chamber wall temperature of approximately 850° C in a next section of the reaction chamber will dissolve approximately 40% of the remaining carbonaceous feedstock into syngas of approximate composition 2CO+02+4H2+guest H2J ; a steam temperature of approximately 800° C and reaction chamber wall temperature of approximately 1000° C in a next section of the reaction chamber towards the distal end will dissolve approximately 20% of the remaining carbonaceous feedstock into syngas of approximate composition CO+CO2+l/202+4H2+H20+guest H2; and, a steam temperature of approximately 1000° C and reaction chamber wall temperature of approximately 1250° C in a final section proximal to the distal end will dissolve approximately 10% of the remaining carbonaceous feedstock into syngas of approximate composition 2C02+4H2+2H20+guest H2.

An exemplary design of a reactor, according to some embodiments of the present invention, may be as follows:

For a feedstock having a normalized bulk density of approximately 1000 kg/m ³ , and assuming a distance between two consecutive flights on the transport mechanism of between 30 cm - 50 cm, a velocity of each flight in any direction is 10 cm/mm, and a residence time of the feedstock in the reactor of 60 minutes, the overall volume of the reactor (reacting chamber) may be estimated to be 90 - 150 litres/mechanical flight.

Assuming the reactor has a diameter 750 mm, a reaction chamber 60 mm wide, 3000 mm high, and a transport mechanism having four flights and a transport rate of 400 kg/hour at the normalized level, the reaction chamber walls would provide 14 m ² of heat transfer surface for the superheating of steam.

The present invention will be understood from the following detailed description of preferred embodiments, which are meant to be descriptive and not limiting. For the sake of brevity, some well-known features, methods, systems, procedures, components, circuits, and so on, are not described in detail.

Reference is now made to Figure 1 which schematically illustrates a single-stage superheating steam gasifier 100, according to an embodiment of the present invention. Gasifier 100 is configured for gasifying carbonaceous materials and non-carbonaceous materials using superheated steam. Optionally, gasifier 100 gasifies mixtures of carbonaceous and non-carbonaceous materials.

In some exemplary embodiments, gasifier 100 includes a size-reducing feed system 1 for reducing the size of feedstock 38. Feedstock material 38 does not require sorting and may be dry or wet, any type of waste, domestic or industrial or medical, clean or contaminated, hazardous for example like cyanides, polyurethanes, may contain, hazardous compositions like dioxins, furanes, PCBs, or may be biomass, wood, coal, plastic of any kind, refinery bottoms and oils, iron and reducing metals, light or heavy, that may be oxygenated, agricultural waste from cattle, poultry, slaughter houses, etc. Optionally, the feedstock material 38 may contain inert materials like glass, sand, stainless steel or pebbles.

In some embodiments, feedstock size reduction allows for feedstock material 38 to easily pass through a gasification reactor 110 in gasifier 100 where syngas is produced. Optionally, feedstock size reduction increases a reacting surface of feedstock material 38 during the process.

In some embodiment, size-reducing feed system 1 is submerged in water for maintaining the material unexposed to the ambient. Optionally, submerging size-reducing feed system

1 in water allows for better controlling a feed rate of the feedstock in the system. Alternatively, size -reducing feed system 1 includes an enclosure (not shown) for sealing the feedstock from the ambient.

In some exemplary embodiments, a mixture funnel feed

2 is used for conducting the size-reduced feedstock into a reactor chamber 10 in reactor 110. In reactor chamber 10, feedstock material 38 is broken down by the superheated steam and syngas is produced.

Reference is now also made to Figure 2 which schematically illustrates a side view of a section of reactor 110, and to Figure 3 which schematically illustrates a cross- sectional top view of the reactor, according to an exemplary embodiment of the invention. Optionally, reactor 110 is cylindrically shaped and includes an outer heating channel 9A and an inner heating channel 9B concentrically extending along a length of the reactor! an outer steam flow channel 5A and an inner steam flow channel 5B also concentrically extending along the length of the reactor; and reactor chamber 10 also concentrically extending along the length of the reactor. Reactor chamber 10 is positioned between outer steam flow channel 5A and inner steam flow channel 5B, and includes inlets 37 on wall 7 of the reaction chamber through which superheated steam flows in counter-flow into the reaction chamber from the outer and inner steam flow channels. Additionally, heat is conducted into reaction chamber 10 from outer steam flow channel 5A and inner steam flow channel 5B through wall 7 of the reactor chamber.

In some exemplary embodiments, outer steam flow channel 5A and inner steam flow channel 5B are adjacently positioned to outer heating channel 9A and inner heating channel 9B _t respectively. Heating gases produced by a heat source 4 flow through outer heating channel 9A and inner heating channel 9B at a substantially high temperature. The heat is conducted from outer heating channel 9A and inner heating channel 9B into outer steam flow channel 5A and inner steam flow channel 5B for transforming saturated steam entering the steam flow channels into superheated steam. Optionally, the superheated steam is at a pressure of 1 atm absolute. In some embodiments, high pressure superheated steam may be pumped into outer steam flow channel 5A and inner steam flow channel 5B, so that outer heating channel 9A and inner heating channel 9B may be eliminated. In some embodiments, heating elements or other heating means may be included in outer steam flow channel 5A and inner steam flow channel 5B so that outer heating channel 9A and inner heating channel 9B may be eHminated.

In some exemplary embodiments, reactor 110 includes a transport mechanism 8 for transporting feedstock material 38 through reactor chamber 10 as it is being broken down into feedstock particles 6 by the superheated steam. Optionally, transport mechanism 8 includes a vibration inducing mechanism 31 for mechanically imparting vibration to feedstock 38 and/or feedstock particles 6 for assisting in breaking down of the material and particles, increasing an efficiency of the gasification process. Additionally or alternatively, vibration inducing mechanism 31 includes a steam pulsator 34 for pulsing the steam and imparting vibratory motion to feedstock material 38 and/or feed particles 6. Additionally or alternatively, vibration inducing mechanism 31 includes an ultrasound generator 35 for pulsing the steam and imparting the vibratory motion to feedstock material 38 and/or feed particles 6. In some embodiments, temperature, pressure, and feedstock transport rate is controlled by a controller 18. Optionally, controller 18 is part of a closed-loop system.

In some exemplary embodiments, non-gasified materials 15 are removed as ash and and/or slag through the distal end of reactor chamber 10. Optionally, the non-gasified materials 15 are removed from gasifier 100 as waste material 16 for landfill and other suitable purposes. In some embodiments, solid residues 17 from steam production are removed through a distal end of outer steam flow channel 5A and inner steam flow channel 5B. Optionally, solid residues 17 are removed from gasifier 100 as part of waste material 16.

In some exemplary embodiments, the saturated steam is produced by a saturated steam boiler 21 from water entering gasifier 100 through a water feed valve 3. Additionally or alternatively, outer heating channel 9A and inner heating channel 9B are connected to a boiler 22 configured for producing the saturated steam using the heat from the heating gas. Optionally, a flue gas exhauster 23 is connected to boiler 22. Optionally, emission control instrumentation 24 is used with flue gas exhauster 23.

In some exemplary embodiments, gasifier 100 includes a filter/neutralizing device 11 to clean a syngas 36 produced from feedstock material 38. Optionally, a neutralizing material feeder 19 connects through a neutralizing material gas-tight gate 20 to filter/neutralizing device 11. A syngas outlet pipe 12 conducts syngas 38 from reactor chamber 10 to filter/neutralizing device 11. Boiler 21 additionally acts as a condenser for de-watering syngas 38, to which a consumer gas pipe is connected for guiding the syngas to a storage facility (not shown) or other destination. In some embodiments, a part of syngas 38 is recycled through a syngas heating pipe 13 to heat source 4 for use as fuel. In some embodiments, a condensate pump 26 pumps the water extracted from condenser 21 to boiler 22 for creating saturated steam.

In some exemplary embodiments, gasifier 100 includes a syngas solids collection plenum 25 with flash cooling and pH controlled water, and with slurry pump for separating the solids. Optionally, a recirculation pump 27 is used for pH control. Additionally or alternatively, gasifier 100 includes a pH and level control tank 28. In some embodiments, a pH controlling solution is added to tank 28 through a control valve 29. Optionally, a water control valve 30 controls water supply to syngas plenum 25 and/or tank 28.

In the figures and/or description herein, the following reference numerals have been mentioned-

Part Ref.

Part Identification No. size-reducing feed system 1

reactor mixture funnel feed 2

make up water feed 3

heat source 4

outer steam flow channel 5A

inner steam flow channel 5B

feedstock particles 6

reactor chamber wall 7

transport mechanism 8

outer heating channel 9A

inner heating channel 9B

reactor chamber 10

filter/neutralizer 11

syngas outlet pipe 12

syngas heating pipe 13

consumer gas pipe 14

non-gasified material 15

landfill waste material 16 steam production solid residues 17

controller 18

neutralizing material feeder 19

neutralizing material gate 20

condenser/boiler 21

boiler 22

flue gas exhauster 23

emission control device 24

syngas solids collection plenum 25

condensate pump 26

pH control recirculation pump 27

pH level control tank 28

pH solution control valve 29

make up water control valve 30

vibration inducing mechanism 31

steam pulsator 34

ultrasound generator 35

syngas 36

reactor chamber apertures (openings) 37

feedstock material 38

gasifier 100

reactor 110

The foregoing description and illustrations of the embodiments of the invention has been presented for the purposes of illustration. It is not intended to be exhaustive or to limit the invention to the above description in any form.

Any term that has been defined above and used in the claims, should to be interpreted according to this definition. The reference numbers in the claims are not a part of the claims, but rather used for facilitating the reading thereof. These reference numbers should not be interpreted as limiting the claims in any form.