NZ617114B2 - Apparatus and methods for tar removal from syngas - Google Patents

Abstract

617114 A process and apparatus are provided for reducing content of tar in a tar containing syngas (150). The process includes contacting the tar containing syngas with a molecular oxygen containing gas (250) in a first reaction zone (200) to produce a gas mixture. The gas mixture is passed through a heat treatment zone (300) maintained at a temperature between about 900°C to about 2000°C for a contact time of about 0.5 to about 5 seconds. In this aspect, at least a portion of the tar undergoes at least partial oxidation and/or cracking to produce a hot syngas (450). a heat treatment zone (300) maintained at a temperature between about 900°C to about 2000°C for a contact time of about 0.5 to about 5 seconds. In this aspect, at least a portion of the tar undergoes at least partial oxidation and/or cracking to produce a hot syngas (450).

Description

APPARATUS AND S FOR TAR REMOVAL FROM SYNGAS This application claims the benefit of US. Provisional Application Nos. 61/516,646, 61/516,704 and 61!516,667 all filed April 6, 2011, all of which are orated in their entirety herein by reference.

An apparatus and method is provided for gasification of carbonaceous materials to produce er gas or synthesis gas or syngas that includes carbon monoxide and hydrogen. More specifically, the apparatus and method are effective for conditioning of producer gas or synthesis gas or syngas and ng tar content of a tar-containing syngas.

BACKGROUND Gasification of carbonaceous materials in an oxygen-starved condition produces syngas (also known as synthesis gas; also known as producer gas) comprising tar.

Presence of tar in syngas poses major technical obstacle in gasification process causing fouling, plugging of downstream processes and equipment. sing tar can ically foul gas cleaning equipment and liquid tar droplets that enter prime movers hamper the operation of these end—use applications of the syngas. Tar in syngas may also greatly impact wastewater management. If tar and condensed water are mixed, e.g., in conventional based gas cleaning s, it may create an often costly and difficult water treatment problem. In order to have a syngas acceptable for downstream processes and equipment content of tar in syngas has to be reduced. Several s of reduction or removal of tar have been disclosed in the published art that include both physical and chemical treatment. Physical treatments for tar removal include use of filter and electrostatic tar removal. Chemical ents include both tic and non-catalytic methods. One method of reducing tar t of syngas is thermal destruction in which tar undergoes one or both of partial oxidation and thermal cracking. See for example: “Tar reduction through partial combustion of fuel gas,” Houben, MP, Lange, H.C. de & Steenhoven, A.A. van, Fuel, vol. 84, pp 817-824, 2005; “Analysis of hydrogen-influence on tar removal by partial oxidation,” Hoeven, TA. van der, Lange, H.C. de & Steenhoven, A.A. van, Fuel, vol. 85, pp 1101-1110, 2005.

In this method, tar containing syngas produced from a gasifier unit is passed through a treatment zone or unit wherein an oxygen—containing gas is added. A high ature in is attained in this unit in order to accomplish tar cracking and/or. partial oxidation. Thus James T. Cobb, Jr. uction of Synthesis Gas by Biomass Gasification," James T. Cobb, Jr., Proceedings of the 2007 Spring National AIChE g, Houston, Texas, April 22-26, 2007) describes a Consutech er (BRI Energy LLC), first stage of which is a standard step-grate combustor ently used as an MSW incinerator) that operates as a gasifier at 950°F using oxygen-enriched air. The second stage is a heat treater that operates at 2000-2250°F and uses minimal oxygen to crack tars. describes a two stage gasifier in which gaseous product fromthe first stage moves to the second stage. Pure oxygen is introduced into the second stage to raise the temperature to about 1750 to about 22500F in order to accomplish one or more of l ion and cracking of tar contained in the s stream from the first stage.

The above described thermal treatment method has been shown to be effective in reducing tar content of syngas in small size unit. There remains a need for developing knowledge for up of this thermal treatment process in order to accomplish effective tar removal in large scale units.

SUMMARY In a first aspect, the present ion provides a process for reducing content of tar in a tar containing syngas, said process comprising: contacting said tar containing syngas with a molecular oxygen containing gas in a first reaction zone to produce a gas mixture; and passing said gas mixture through a heat treatment zone maintained at a temperature between about 900°C to about 2000°C for a contact time of about 0.5 to about 5 seconds wherein at least a portion of the tar undergoes at least partial oxidation and/ or cracking to produce a hot syngas; wherein the gas e from the first reaction zone changes direction of flow by impingement on a surface.

In a second aspect, the present invention provides a process for reducing content of tar in a tar containing syngas, said process comprising: contacting said tar containing syngas with a molecular oxygen containing gas in a first reaction zone to produce a gas mixture, wherein a linear velocity ofa flow of said tar containing syngas oxygen mixture at an exit of said first reaction zone is r than about 5 meters per second; and g said gas mixture through a heat treatment zone maintained at a temperature (T) between about 900°C to about 2000°C for a t time (Ct) of about 0.5 to about 5 seconds wherein at least a portion of the tar undergoes at least partial ion and/ or cracking to produce a hot syngas; and changing direction of gas flow from the first reaction zone; wherein the tar concentration equivalent content of the hot syngas is maintained at less than 10ppm, wherein 10724692_1 a ratio of linear velocity (meters/second) to height (meters) of the heat treatment zone is about 0.3:12.5 to about 2.0:2.5.

In a third aspect, the present invention provides syngas obtained by the method according to the first aspect or the second aspect.

A s is provided for reducing content of tar in a tar ning syngas. The process includes contacting the tar containing syngas with a molecular oxygen containing gas in a first on zone to produce a gas mixture. The gas mixture is passed through a heat treatment zone maintained at a temperature between about 900°C to about 2000°C for a contact time of about 0.5 to about 5 seconds. In this , at least a portion of the tar undergoes at least partial ion and/or cracking to produce a hot . The gas e from the first reaction zone changes direction of flow by impingement on a surface. In one aspect, a linear velocity of a flow of the tar containing syngas oxygen mixture at an exit of the first reaction zone is greater than about 5 meters per second. At least a n of hot syngas may be introduced into the first reaction zone. In another aspect, a ratio of linear velocity to height of the heat treatment zone is about 0.3:12.5 to about 2.0:2.5. In one aspect, the heat treatment zone includes: (a) a first heat treatment zone effective for thermal treatment of tar contained in the gas mixture to produce a less tar ning gas mixture; and (b) a second heat treatment zone effective for thermal treatment of tar contained in said less tar containing gas mixture to produce hot syngas.

A tar removal apparatus is provided that is effective for reducing content of tar in a tar ning syngas to produce a hot syngas. The tar removal apparatus includes: (a) a 10724692_1 first reaction zone wherein molecular oxygen is introduced and mixed with said tar containing syngas to produce a gas mixture; and (b) a heat ent zone for thermal treatment of tar contained in the gas mixture. The gas mixture from the first reaction zone changes ion of flow by impingement on a surface. The heat treatment zone provides a contact time of about 05 to about 5 seconds. In one aspect, the first reaction zone provides a linear velocity of flow of the tar containing syngas oxygen mixture r than about 5 meters per second at the exit of the first reaction zone. In another aspect, the heat treatment zone of the tar removal apparatus includes: (a) a first heat treatment zone for l ent of tar contained in the gas mixture to produce a less tar containing gas mixture; and (b) a second heat treatment zone for therma} treatment of tar ned in the less tar containing gas mixture to produce hot syngas. The tar removal apparatus is effective for providing a gas mixture from the first reaction zone that es on a e in less than about 2 seconds.

A syngas production apparatus is ed that includes (a) a gasification zone wherein a carbonaceous material is contacted with molecular oxygen and optionally contacted with one or more of steam and carbon dioxide to produce a tar containing syngas; (b) a first reaction zone wherein molecular oxygen is introduced and mixed with the tar containing syngas to produce a gas mixture; and (c) a heat ent zone for thermal treatment of tar contained in the tar containing syngas oxygen mixture. The tar containing syngas oxygen mixture from the first reaction zone changes direction of flow by impingement on a surface and the heat ent zone provides a contact time of about 0.5 to about 5 seconds.

A process for reducing content of tar in a tar containing syngas is provided. The process includes: contacting said tar containing syngas with a molecular oxygen containing gas in a first reaction zone to produce a gas e; and passing the gas mixture through a heat treatment zone at a temperature and for a time effective for reducing tar content of the syngas by at least about 10%. The gas mixture from the first reaction zone changes direction of flow by impingement on a surface.

BRIEF DESCRIPTION OF S The above and other s, features and advantages of several aspects of the process will be more apparent from the following drawings.

Figure l is a schematic m of a tar reduction apparatus for reducing tar content of a tar containing syngas. Figure 1 illustrates one aspect of the apparatus that includes a First reaction zone and a Heat Treatment Zone.

Figure 2 is a schematic diagram of a tar reduction apparatus for reducing tar content of a tar containing syngas. Figure 2 illustrates one aspect of the apparatus that includes a First reaction Zone and 21 Heat ent Zone sing Heat Treatment Zone I and Heat Treatment Zone II.

Figure 3 is a schematic diagram of a gasification apparatus for ng tar content of a tar containing syngas. Figure 3 illustrates one aspect of the apparatus that es a Gasification Zone, a First reaction zone and a Heat Treatment Zone that includes 21 Heat Treatment Zone I and Heat Treatment Zone II.

Figure 4 presents side and top views of aspects of the first reaction zone wherein the first reaction zone is cylindrical in shape. Figures 4 (I) & 4 (II) present side views of aspects of the first reaction zone wherein the first reaction zone is vertical and gas inlet for molecular oxygen is inclined at an angle to horizontal line. Figures 4 (III) & 4 (IV) t top views or cross sections of aspects of the first reaction zone n the first reaction zone is vertical and gas inlet for molecular oxygen is ed at an angle to a diagonal drawn through point of intersection of the cross section and axis of the gas inlet.

Figure 5 presents side and top views of an aspect of the first reaction zone wherein the first reaction zone is a vertical cylindrical vessel with eight gas inlet nozzles ed to it for introducing molecular oxygen.

Figure 6 presents side views of aspects of the first reaction zone. Figures 6 (i) & 6 (II) present side views of aspects of the first on zone wherein the first reaction zone is inclined at an angle to a vertical tine.

Corresponding reference characters te corresponding components throughout the several views of the drawings. Skiiled artisans will appreciate that elements in the figures are illustrated for simplicity and clarity and have not necessarily been drawn to scale. For example, the dimensions of some of the elements in the figures may be exaggerated ve to other elements to help to improve understanding of various aspects of the present process and apparatus. Also, common but well-understood elements that are useful or necessary in commercially feasible aspects are often not depicted in order to facilitate a iess obstructed view of these s aspects.

DETAILED DESCRIPTION Definitions Unless otherwise defined, the following terms as used throughout this specification for the t disclosure are defined as follows and can include either the ar or plural forms of definitions below defined: The term “about" modifying any amount refers to the variation in that amount encountered in real world conditions, e.g., in the lab, pilot plant, or tion facility. For example, an amount of an ingredient or measurement employed in a mixture or quantity when modified by “about” includes the variation and degree of care lly employed in measuring in an experimental condition in production plant or lab. For example, the amount of a component of a product when d by “about” includes the variation between batches in a multiple experiments in the plant or lab and the variation inherent in the analytical method. Whether or not modified by “about,” the amounts include lents to those amounts. Any quantity stated herein and modified by “about” can also be employed in the present disclosure as the amount not modified by “about”.

“Carbonaceous material” as used herein refers to carbon rich material such as coal, and petrochemicals. r, in this specification, carbonaceous material includes any carbon material whether in solid, liquid, gas, or plasma state. Among the us items that can be considered aceous material, the present disclosure contemplates: carbonaceous material, carbonaceous liquid product, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (MSW or msw), carbonaceous urban waste, aceous agricultural al, carbonaceous forestry material, carbonaceous wood waste, carbonaceous construction material, carbonaceous tive material, carbonaceous industrial waste, carbonaceous fermentation waste, aceous petrochemical co-products, carbonaceous alcohol production co—products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersoft, lignin, black liquor, polymers, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residues, wood processing residues, livestock wastes, poultry wastes, food processing residues, fermentative process wastes, ethanol coproducts, spent grain, spent microorganisms, or their combinations.

The term “fibersoft” or “Fibersoft”or “iibrosoft” or “fibrousoft” means a type of carbonaceous material that is produced as a result of softening and concentration of various nces; in an example carbonaceous material is produced via steam aving of various substances. In another example, the fibersoft can comprise steam autoclaving of municipal, industrial, commercial, medical waste resulting in a fibrous mushy material.

The term “municipal solid waste” or “MSW” or “msw” means waste comprising household, commercial, industrial andfor residual waste.

The term “syngas” or “synthesis gas” means synthesis gas which is the name given to a gas mixture that contains varying amounts of carbon monoxide and hydrogen.

Examples of production methods e steam reforming of l gas or hydrocarbons to produce hydrogen, the gasification of coal and in some types of waste—to-energy gasification ties. The name comes from their use as intermediates in creating synthetic natural gas (SNG) and for ing ammonia or methanol. Syngas comprises use as an intermediate in producing synthetic petroleum for use as a fuel or lubricant via Fischer—Tropsch synthesis and previously the Mobil ol to gasoline process. Syngas consists primarily of hydrogen, carbon monoxide, and some carbon dioxide, and has less than half the energy density (i.e., BTU t) of natural gas. Syngas is combustible and often used as a fuel source or as an intermediate for the production of other als.

“Ton” or “ton” refers to US. short ton, i.e. about 907.2 kg (2000 lbs).

As used herein, the term "tar" includes, without tion, a gaseous tar, a liquid tar, a solid tar, a tar-forming substances, or mixtures thereof, which generally comprise hydrocarbons and derivatives thereof. A large number of well known tar measurement methods exist that may be utilized to measure tar. One large family of techniques es analytical methods based on liquid or gas phase chromatography coupled with a detector.

The most frequent detectors in the case of measurement of tars are the flame-ionization detector (FID) and the mass spectrometer. Another family of techniques includes spectrometric methods, which include detecting and analyzing a um. This is for example ed, ultraviolet (UV) or luminescence spectrometry, and LIBS (Laser— induced Breakdown Spectroscopy) technique. r technique for monitoring of combustion gases is FTlR (Fourier Transform InfraRed) infrared spectrometry.

Miscellaneous documents mention this technique, such as for example W020060l5660, WOO3060480 and US. Pat. No. 5,984,998.

There exist other known electronic methods which allow continuous monitoring of tars. These techniques include detectors with electrochemical cells and sensors with nductors. Various gravimetric techniques may also be ed for tar measurements. In one aspect, the amount of tar may be expressed as equivalent ppm of carbon. In this aspect, the hydrocarbon may be benzene or an alcohol, such as methanol. In this aspect, reducing content of tar may mean a tar concentration equivalent or tar equivalents corresponding to less than about 10 ppm benzene.

Detailed Description The following description is not to be taken in a limiting sense, but is made merely for the purpose of describing the l ples of exemplary embodiments. The scope of the ion should be ined with reference to the claims.

Apparatus and methods for treatment of tar containing syngas to reduce its tar content are provided. In another aspect, apparatus and methods for gasification of carbonaceous material to produce a tar ning syngas and subsequent heat treatment of said tar containing syngas are provided. Various aspects of the tus of this disclosure are illustrated in Figures 1 to 3.

Figure 1 is a schematic diagram of one aspect of a tar reduction apparatus (10) for reducing tar content of a tar containing syngas. Figure 1 illustrates one aSpect of the apparatus that es a First Reaction Zone (200) and 21 Heat Treatment Zone (300).

Referring now to Figure 1, tar containing syngas (150) and molecular oxygen containing gas (250) are introduced into said first reaction zone. A gas mixture (mixture of tar containing syngas and molecular oxygen) is produced in the first reaction zone that enters the heat treatment zone (not shown on diagram). A stream of hot syngas (450) is removed from the heat treatment zone.

Figure 2 is a schematic diagram of one aspect of a tar reduction apparatus (11) for reducing tar content of a tar containing syngas. Figure 2 illustrates one aspect of said apparatus comprising a First Reaction Zone (200) and a Heat Treatment Zone comprising Heat Treatment Zone I (300) and Heat Treatment Zone Ii (400). Referring now to Figure 2, tar containing syngas (150) and molecular oxygen containing gas (250) are introduced into said first reaction zone. A gas mixture re of tar containing syngas and molecular oxygen) is ed in the first reaction zone that enters the heat treatment zone I (not shown on diagram). A heat treated gas mixture leaves heat treatment zone I and enters heat treatment zone II. A stream of hot syngas (450) is removed from the heat treatment zone II.

Figure 3 is a schematic diagram of a gasification apparatus (12) for reducing tar t of a tar containing . Figure 3 illustrates one aspect of said apparatus comprising a Gasification Zone (100), a First Reaction Zone (200) and a Heat Treatment Zone sing Heat Treatment Zone I (300) and Heat Treatment Zone 11 (400).

Referring now to Figure 3, carbonaceous material feed (110) and lar oxygen containing gas (120) are introduced into the gasification zone that produces a tar ning syngas (not shown on diagram). Said tar containing syngas and molecular oxygen containing gas (250) are introduced into the first reaction zone. A gas mixture (mixture of tar containing syngas and molecular oxygen) is produced in the first reaction zone that enters the heat treatment zone I (not shown on m). A heat treated gas mixture leaves heat treatment zone I and enters heat ent zone.

Thus the tar treatment apparatus includes a first reaction zone and a heat treatment zone. Tar containing syngas feed is passed through the first reaction zone. The first reaction zone can be a small pipe section or a small vessel of any cross section including but not limited to circular or rectangular cross section one end of which is attached to the heat treatment zone. In one aspect, the cross section of the first reaction zone is circular. In one aspect, the first reaction zone is positioned vertically.

A molecular oxygen containing gas is introduced into the first reaction zone. One or more gas inlets (nozzles) might be ed to the first reaction zone for introduction of molecular oxygen containing gas. One or more of said nozzles can be positioned perpendicular to the axis of the first reaction zone as shown in Figures 4 (l) & 4 (11).

Figure 4 (1) illustrates an aspect of the first reaction zone wherein gas inlet for molecular flow direction. Figure oxygen is inclined at an angle or to horizontal line with a downward 4 (I) ts a side View of an aspect of the first on zone wherein the first reaction zone is vertical and gas inlet for moiecuiar oxygen is inclined at an angle 0!. to horizontal tine with a downward flow direction. Figure 4 (II) illnstrates an aspect of the first reaction zone wherein gas inlet for molecular oxygen is inclined at an angle 0!. to ntal line with an upward flow direction. Figure 4 (II) presents a side View of an aspect of the first reaction zone wherein the first reaction zone is vertical and gas inlet for molecular oxygen is inciined at an angle or to horizontal line with an upward flow direction.

One or more of said s can be oned obliquely to a diagonal drawn through point of intersection of the surface of the first reaction zone and axis of the gas inlet and positioned in a way that facilitates formation of swirl inside the mixing zone. s 4 (III) & 4 (IV) respectively present top Views or cross sections of an aspect of the first reaction zone wherein the first reaction zone is vertical and gas inlet for molecular oxygen is inclined at an angle [3 to a diagonal drawn h point of intersection of the cross section and axis of the gas inlet.

Figures 5 (I) & 5 (II) respectively present side and top views tively of an aspect of the first reaction zone wherein the first reaction zone is a vertical cylindrical vessel with eight gas inlet nozzIes attached to it for introducing molecular oxygen. Each nozzle is d at an angle or with horizontal direction with an upward direction of gas flow. Each nozzle is mounted at an angle 8 to a diagonal of cross section drawn through point of ection of nozzle and first reaction zone.

In various aspects, the first on zone can be positioned at an angle to the vertical direction Figures 6 (I) & 6 (II) respectively present side views of aspects of the first reaction zone wherein the first reaction zone is inclined at an angle 9 to a vertical line.

The heat treatment zone is a vessel of any cross section including but not d to circular, , rectangular, etc. In one aspect, the heat treatment zone is positioned substantially vertically. In one , the heat treatment zone is positioned substantially horizontally. In one aspect, the heat treatment zone is positioned at an angle to the horizontal direction. In one aSpect, the heat treatment zone ses multiple sections or sub—zones. In one aspect, the heat treatment zone comprises two sections or sub-zones: Heat Treatment Zone I and Heat Treatment Zone II. In one aspect heat treatment zone I is ntal. In one aspect heat treatment zone I is vertical. In one aSpect heat treatment zone II is ntal. In one aspect heat treatment zone II is vertical. In one aspect, heat transfer zone I is positioned at an angle to the horizontal direction. In one aspect, heat transfer zone II is positioned at an angle to the ntal ion. In one aspect, heat er zone I is positioned at an angle to the vertical direction. In one aspect, heat transfer zone 11 is positioned at an angIe to the vertical direction.

In one aspect, a tar containing syngas is subjected to heat treatment in a heat treatment zone in order to accomplish destruction of tar by one or more of cracking and partiai oxidation wherein said tar containing syngas is mixed with molecular oxygen containing gas prior to introduction in the heat treatment zone. Mixing is accomplished in a first reaction zone through which tar containing syngas is introduced into said heat treatment zone. Effectiveness of heat treatment in heat treatment zone can depend on effectiveness of mixing. Effectiveness of heat treatment can be ed by attaining a specified minimum linear velocity of gas mixture (tar containing syngas oxygen mixture) entering the heat treatment zone. Effectiveness of heat treatment can be improved by changing the direction of flow of the gas mixture as it enters the heat treatment zone. iveness of heat treatment can be improved by impingement on a surface as it enters the heat treatment zone. Effectiveness of heat treatment can be improved by ng direction of flow of gas mixture entering the heat treatment zone by impingement on a surface. In one , effectiveness of heat treatment can be improved by impingement of the gas mixture from the first reaction zone on a surface of the heat treatment zone.

In one aspect, a linear velocity of gas mixture at the exit of the first reaction zone is at least 5 meters/second. In one aSpect, a linear velocity of gas mixture is at least 10 meters/second. In one aspect, a linear velocity of gas mixture is at least 15 meters/second.

In one aspect, a linear velocity of gas mixture is at least 20 meters/second. In one aspect, a iinear velocity of gas mixture is at feast 25 /second. In one aspect, a linear velocity of gas mixture is at least 50 meterstsecond. The height of the heat treatment zone may be in a range of from about 1 meter to about 15 meters. In another aspect, a ratio of linear velocity to height of the heat treatment zone is about 03:12.5 to about 2.02.5. In various aspects, the ratio of linear velocity to height of the heat treatment zone may be ed from 5, 04:10.0, 0.5:7.5, 25, 0.8150, 104.0, 1.25:3.75, 1.53.3, 1.73.0, and 2,012.5. Linear velocity is measured at the exit of the first reaction zone. If the heat treatment zone is square or rectangular, then the height is the inside height. If the heat treatment zone is circular, than the height is the inside diameter. In another aspect, the gas mixture from the first reaction zone impinges on a surface in less that about 2 seconds, in another aspect less than about 1 second, in another aspect less than about 0.5 seconds, and in another aspect less than about 0.1 seconds.

Factors that can affect mixing and performance of heat treatment include but are not limited to mixing length provided by the first reaction zone (cg. height of first reaction zone), shape and cross sectionai area of first reaction zone, ratio of molecular oxygen containing gas to tar containing syngas, ratio of length to er of first reaction zone downstream of the oxygen inlet. Number and orientation of gas inlets (nozzles) for introducing moiecular oxygen containing gas can influence . Mixing can also be improved by inserting mixing devices inside first reaction zone such as baffles or motionless mixers. Mixing and performance of heat treatment can be improved by increasing flow rate of gas through the first reaction zone or heat ent zone. For example in one aspect, performance of heat treatment can be improved by recycling a portion of syngas g the heat treatment zone (hot syngas). In r aspect, performance of heat ent can be improved by feeding tar containing raw syngas from more than one source through one first reaction zone and one heat treatment zone. In one aspect, performance of heat treatment can be improved by feeding tar containing raw syngas from more than one gasifier through one first reaction zone and one heat treatment zone.

In order to accomplish one or more of l oxidation and ng of tar, the heat treatment zone is maintained at a temperature n about 900°C to about 2000". In one aspect, the temperature is n about 1000°C and about 1700°C. In one aspect, the temperature is between about 1100°C and about 1500°C. In one aspect, the temperature is between about I200°C and about 1250°C.

In order to accomplish one or more of l oxidation and cracking of tar effectively, the contact time in the heat treatment zone is n about 0.5 to about 5 s. In these aspects, the process is effective for reducing the tar content of the syngas by at least about 10%.

The molecular oxygen containing gas may comprise air. The lar oxygen containing gas may comprise oxygen enriched air. The molecular oxygen containing gas added in the tar ion may comprise pure oxygen. Total amount of molecular oxygen zone can be in a range of about 0 to about 100 1b—moles per dry ton of carbonaceous material on a dry basis.

The gasification zone of the present disclosure may be any gasification equipment disclosed in prior art such as and not limited to moving bed, fixed bed, fluidized bed, entrained flow, counter—current ("up draft"), co—current (”down draft”), counter—current fixed bed, co—current fixed bed, counter-current moving bed, co—current moving bed cross draft, hybrid, cross flow, cross flow moving bed, or a part thereof, or combinations thereof. In one aspect, the gasification zone is a cross flow moving bed unit. In one aspect, the gasification zone comprises two or more units or sections or hearths for contacting said carbonaceous material with molecular oxygen~containing gas and optionally with one or more of steam and C02 to gasify said carbonaceous material and to produce a tar containing syngas. In various aspects, the gasification zone comprises 1, 2, 3, 4, 5, 6, 7, 8, 9, or 10 units or sections or s.

Gas inlets for introduction of molecular oxygen containing gas can be ed to the gasification zone or one or more sections or units or hearths contained therein. Steam molecular oxygen or CO; may also be introduced, optionaily through one or more of these inlets. In one aspect, one or more of molecular oxygen containing gas, steam and C02 may be introduced through the gas inlets attached to the gasification zone or to one or more hearths or sections or units ned therein. In one , one or more of molecular oxygen containing gas, steam and C02 are pre-mixed prior to supplying to the gas inlets attached to the ation zone or to one or more hearths or sections or units contained therein.

A carbonaceous material feed is introduced in the gasification zone. A molecular oxygen containing gas is supplied to the gasification zone. Thus the aceous material feed is treated with molecular oxygen in order to initiate and facilitate chemical transformation of carbonaceous material. Carbonaceous material feed is gasified in the gasification zone to produce a tar ning syngas. Supply of oxygen) into the gasification apparatus is controlled in order to preferentially promote formation of carbon monoxide from carbonaceous material. A sub—stoichiometric amount of oxygen is supplied in order to promote production of carbon monoxide. A stream of tar containing syngas is removed from the gasification zone.

A high enough temperature is attained in the gasification zone to facilitate gasification of carbonaceous al. However, the temperature is maintained low enough so that nonucarbonaceous mineral matter contained in carbonaceous material feed does not melt inside the gasification zone. In other words, the ature in any part of the gasification zone may not exceed the melting point temperature of ash comprising said non—carbonaceous mineral matter. Typically, a temperature not exceeding 800°C is maintained in the gasification zone as well as in the p zone. In one aspect, temperature in the gasification zone is maintained in 250°C—800°C range. Thus solid ash comprising said non-carbonaceous l matter accumulates in the gasification zone and a stream of solid ash is removed from the gasification zone. In s aspects, temperature in the gasification zone can be in 250°C-800°C range, in 450°C—800°C range, in 650°C-800°C range.

In order to supply molecular oxygen said molecular oxygen containing gas may se air. In order to supply molecular oxygen said molecular oxygen containing gas may comprise enriched air. In order to supply molecular oxygen said molecular oxygen containing gas may comprise pure oxygen.

Total amount of molecular oxygen introduced in the gasification zone through said molecular oxygen containing gas can be in a range of about 0 to about 50 lb—moles per ton of carbonaceous material on a dry basis. Total amount of steam introduced in the gasification zone can be in a range of about 0 to about 100 es per ton of carbonaceous material feed on a dry basis, and in another aspect, about 0 to about 50 lb- moles per ton of carbonaceous material feed on a dry basis. Total amount of carbon dioxide gas introduced in the gasification zone can be in the range of about 0 to about 50 lb—moles per ton of carbonaceous material feed on a dry basis. In one , both steam and carbon dioxide gas are introduced in the gasification zone. In one aspect, one or more of steam and carbon dioxide gas are injected in one or more lines supplying oxygen to blend in with oxygen lines just before distribution nozzle.

The carbonaceous material fed to the gasification zone may comprise selection from: carbonaceous al, carbonaceous liquid product, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (MSW or rnsw), carbonaceous urban waste, carbonaceous agricultural material, carbonaceous ry material, carbonaceous wood waste, carbonaceous construction material, carbonaceous vegetative material, carbonaceous industrial waste, carbonaceous fermentation waste, carbonaceous petrochemical co-products, carbonaceous l production co—products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersoft, lignin, black liquor, rs, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residues, wood processing residues, ock wastes, poultry wastes, food processing residues, fermentative process wastes, ethanol co—products, spent grain, spent microorganisms, or their combinations.

In one aspect of the present disclosure the carbonaceous material fed to the gasification zone comprises a plurality of carbonaceous materials selected from carbonaceous material, carbonaceoas liquid t, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (MSW or msw), carbonaceous urban waste, carbonaceous agricultural al, carbonaceous forestry material, carbonaceous wood waste, carbonaceous construction material, carbonaceous vegetative material, carbonaceous rial waste, carbonaceous tation waste, carbonaceous hemical co-products, carbonaceous alcohol production co-products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersoft, lignin, black , polymers, ‘waste polymers, polyethylene terephthalate , polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residues, wood processing residues, livestock , poultry wastes, food processing residues, fermentative process wastes, ethanol ducts, spent grain, spent microorganisms, or their combinations.

While the invention herein disclosed has been described by means of specific embodiments, es and applications thereof, numerous modifications and variations could be made thereto by those skilled in the art without departing from the scope of the invention set forth in the claims.

Claims (12)

1. A process for reducing content of tar in a tar containing syngas, said process comprising: ting said tar containing syngas with a molecular oxygen containing gas in a first reaction zone to produce a gas mixture; and passing said gas mixture through a heat ent zone ined at a temperature between about 900°C to about 2000°C for a contact time of about 0.5 to about 5 seconds wherein at least a portion of the tar undergoes at least partial oxidation and/ or cracking to produce a hot syngas; wherein the gas mixture from the first reaction zone changes direction of flow by impingement on a surface.

2. The process of claim 1 wherein said heat treatment zone is maintained at a ature between about 1000°C to .

3. The process of claim 1 or claim 2 wherein said heat treatment zone is maintained at a temperature between about 1200°C to 1250°C range.

4. The process of any one of claims 1 to 3 wherein a linear velocity of a flow of said tar containing syngas oxygen e at an exit of said first reaction zone is greater than about 5 meters per second.

5. The process of any one of claims 1 to 4 further comprising introducing at least a portion of hot syngas into the first reaction zone.

6. The process of claim 4 wherein a ratio of linear velocity (meters/second) to height of the heat treatment zone (meters) is about 0.3:12.5 to about 2.0:2.5.

7. The process of any one of claims 1 to 6 wherein the heat treatment zone comprises: (a) a first heat treatment zone effective for thermal treatment of tar ned in the gas mixture to produce a less tar ning gas mixture; and (b) a second heat treatment zone effective for thermal treatment of tar contained in said less tar containing gas mixture to produce hot . (10724687_1):MGH

8. The process according to claim 1, sing: treating a carbonaceous material with a molecular oxygen containing gas and ally with one or more of steam and carbon dioxide in a gasification zone to produce a tar ning syngas; passing said tar containing syngas and a molecular oxygen containing gas through a first reaction zone to produce a gas mixture, wherein a linear velocity of a flow of said tar containing syngas oxygen mixture at an exit of said first reaction zone is r than about 5 meters per second; and g said gas mixture through a heat treatment zone maintained at a temperature of about 900°C to about 2000°C for a contact time of about 0.5 to about 5 seconds range wherein at least a portion of the tar undergoes one or more of partial oxidation and cracking to produce a hot syngas; wherein the gas mixture from first reaction zone changes ion of flow by impingement on a surface, wherein a ratio of linear velocity (meters/second) to height (meters) of the heat treatment zone is about 0.3:12.5 to about 2.0:2.5.

9. The process according to claim 1, comprising: contacting said tar containing syngas with a molecular oxygen containing gas in a first reaction zone to produce a gas mixture, n a linear ty of a flow of said tar containing syngas oxygen mixture at an exit of said first reaction zone is greater than about 5 meters per second; and passing said gas mixture through a heat treatment zone at a temperature and for a time effective for reducing tar content of the syngas by at least about 10%; wherein the gas mixture from the first reaction zone changes direction of flow by impingement on a surface, wherein a ratio of linear velocity (meters/second) to height (meters) of the heat treatment zone is about 0.3:12.5 to about 2.0:2.5.

10. A process for ng content of tar in a tar containing syngas, said process comprising: contacting said tar ning syngas with a molecular oxygen containing gas in a first reaction zone to produce a gas mixture, n a linear velocity of a flow of said tar (10724687_1):MGH containing syngas oxygen mixture at an exit of said first reaction zone is greater than about 5 meters per second; and passing said gas mixture through a heat treatment zone maintained at a temperature (T) between about 900°C to about 2000°C for a contact time (Ct) of about 0.5 to about 5 seconds wherein at least a portion of the tar undergoes at least l oxidation and/ or cracking to produce a hot syngas; and changing direction of gas flow from the first reaction zone; wherein the tar concentration equivalent content of the hot syngas is maintained at less than 10ppm, n a ratio of linear velocity (meters/second) to height (meters) of the heat ent zone is about 0.3:12.5 to about 2.0:2.5.

11. The process of claim 10 wherein the tar concentration equivalent t of the hot syngas is maintained at less than 10 ppm through control of the temperature (T) and/ or the contact time (Ct).

12. Syngas obtained by the method according to claim 1 or claim 10.