CN1260001C - Feed nozzles for gasification reactors for halogenated substances - Google Patents

Abstract

A method and apparatus for feeding a halogenated substance into a gasification reactor comprises supplying a gas source of oxygen at a supersonic velocity and discharging the liquid halogenated substance from at least one discharge port, wherein the discharge port is radially located around the discharged oxygen source gas so that the oxygen source gas atomizes the liquid halogenated substance and enters the gasification reactor.

Description

Feed nozzles for gasification reactors for halogenated substances

This invention relates to feed nozzles, sometimes referred to as burners, for gasification reactors, and more particularly to gasification reactor feed nozzles for halogenated substances, especially halogenated organics and chlorinated organics (RC1).

Related inventions include a prior patent application for a method and apparatus for producing one or more useful products from low-value halogenated substances, published on July 1, 1999, International Publication No. WO 99/32937 PCT International Application PCT/US/98/26298. This PCT application discloses the conversion of feedstocks consisting essentially of halogenated species, especially by-products, and Process and apparatus for converting waste chlorinated hydrocarbons produced into one or more "high value products".

In general, the gasification reactor for halogenated species preferably comprises a refractory lined cylindrical vessel with a mixing nozzle attached at one end. The halogenated substance, usually a mixture of RC1 or various substances, oxygen and most likely steam, and optionally additional gaseous fuel, water/hydrogen halide vapor and _CO2 are fed into the gasification reactor through the feed nozzle And atomized to generate gaseous partial oxidation products. A typical set of operating conditions includes a liquid (optionally preheated or pretreated) halogenated hydrocarbon feed at a flow rate of approximately 170 L/min (45 GPM) at approximately 30°C and a standard pressure of 7 bar (100 psig). ). Oxygen was supplied at approximately 450 kg (10,000 lbs)/hour at 120°C and 14 bar (200 psig) pressure. Steam and oxygen are supplied at a rate of approximately 450 kg (10,000 lbs) per hour and are saturated at a pressure of 10 bar (150 psig). The reactor pressure is 5 bar (75 psig) and the reactor temperature is preferably between 1300°C and 1500°C.

Proper dispersion of the liquid halogenated feedstock material fed to the partial oxidation (gasification) reactor is a critical step for the successful operation of the gasification process. The operating objectives of the dispersing nozzle (sometimes referred to as the burner) include the difficult goal of stable operation of the reactor over a wide range of feedstock materials, while nearly completely reacting the halogenated species, and minimizing partially reacted feedstock. The overall requirements placed on reactor feed nozzles in increasingly harsh gasification environments do present difficult operating constraints. For comparison, even in the related field of coal gasification a more benign environment than considered here is proposed or provided, nozzle design and performance are known to be limiting factors for reactor reliability.

For example, the RC1 gasification process presents unique problems when compared to coal gasification processes, or even to the gasification of other carbon-containing non-halogenated species. On the one hand, halogenated substances, such as hydrogen chloride, are very corrosive. Second, the feed stream to a gasification reactor of a liquid, such as liquid RC1, has different properties compared to many conventional gasification processes. For optimal operation of a halogenated species gasification reactor, many different feed streams of the halogenated species must be supplied. There is a need for multiple feed conduits from multiple sources of halogenated species and, if fed simultaneously, a configuration of the conduits that avoids unwanted reactions of the multiple feed streams with each other within the nozzle.

For gasification reactor purposes, prior art feed nozzles tend to utilize internal mixing within the nozzle, helping to ensure efficient breakdown of the liquid stream. For example, internal mixing nozzles are known for fuel oil atomization and it is believed that this application yields the highest operating efficiencies. However, internal mixing is not the preferred method in the current environment. Internal mixing of halogenated species and oxygen into the nozzle raises safety and reactivity concerns. Internal mixing within the nozzle contaminates the inside of the nozzle after shutdown, and feed tar during shutdown may coat the interior of the nozzle. This contamination may cause oxidation reactions within the nozzle. It is therefore an object of the present invention to obtain effective external mixing nozzles which are better in terms of safety and reactivity. These considerations outweigh the added complexity and/or lower atomization efficiency and/or high pressure drop of oxygen of a multi-port design. At the same time, however, it should be realized that elegant simplicity of design is always a desired advantage of mixing nozzles to enable higher gasifier reliability. Simplicity of design is also cited here as an advantage, but this is subject to real operating constraints.

As mentioned above, the feed nozzle or burner is an important component of the integrity of the gasification reactor. The discharge jet from the burner is the momentum source for mixing within the gasifier, and the main burner must atomize the liquid fuel into this mixing jet. A typical atomization performance target is 99% of the liquid volume atomized to a droplet size of 500 microns or smaller. This provides sufficient liquid surface area to enable rapid evaporation of the fuel. Two mechanisms operate during this atomization. In a preferred embodiment, liquid is injected through a ring-shaped array of holes centrally located around a central oxygen discharge, and the pressure drop across these holes initiates the process of coarse atomization of discrete liquid jets. Accordingly, the orifice and the liquid jet intersect preferably in front of the burner face, more specifically along the axis of the oxygen discharge with the oxygen discharge jet. In this mode, the oxygen exhaust jet provides the main energy for the fine atomization. The static pressure of oxygen is converted into kinetic energy by the burner nozzle. The nozzles are preferably close to sonic, or more preferably supersonic, so that maximum velocity can be achieved. The difference in velocity between gas and liquid is the atomization energy that breaks up the liquid jet into fine, discrete droplets. In a preferred mode of operation a steam moderator stream can be mixed with the oxygen upstream of the burner. The oxygen entering the gasifier is preferably preheated to 120°C to compensate for the temperature drop as the oxygen expands through the nozzle, thus increasing atomization efficiency.

Another aspect of the present invention is the use of the expansion energy of the oxygen source gas exiting through the nozzle to externally decompose and finely atomize the impinging liquid feed stream. The advantageous use of gas expansion energy mixes the oxygen source gas with the external impinging liquid stream into the feed nozzle and fully atomizes the external liquid into the nozzle. The design utilizes the available work derived from expanding oxidizing gas which is contracted and then expanded preferably through the gas channels formed by the internal nozzle structure to energize, atomize and inject liquid fuel into the reactor chamber. The oxygen source gas may be oxygen, steam and/or another gas. Usually the gas is pure oxygen. The preferred converging then diverging design of the oxygen channel maximizes the exit velocity of the gas. One aspect of the present invention is the configuration and operation of the converging-expanding oxygen passage to obtain an acoustic flow of oxygen source gas at the end of the constricting section. Ultrasonic flux is then obtained in the subsequent channel expansion section. (However, narrowing-only nozzles may be used selectively, especially if the oxygen source gas cannot be accelerated enough due to pressure ratios to operate at a sonic flow rate within a shrinking-diverging nozzle design. Generally, although narrowing-only nozzles can be used Reduced nozzle design, but its smaller efficiency should be taken into account.)

Flame temperatures in excess of 3000°C can achieve mixing of the oxygen source gas and the halogenated species feed. This temperature, although achieved at the slightly downstream end of the nozzle, can radiate energy backwards, heating the downstream portion of the nozzle, and possibly shortening the life of the nozzle. Therefore, the cooling of the tip portion of the nozzle or the downstream end portion of the nozzle is another aspect of the design. Cooling is done by several methods including vapor film cooling of the outside of the nozzle housing and/or providing a circuit of cooling medium (eg water) in the housing part of the nozzle itself. Water cooled jackets (albeit more complex than steam film cooling) offer an additional proven design to the feed nozzle industry, which is also disclosed herein as an additional cooling system. Vapor film cooling jackets offer the advantage of controlling metal surface temperatures with simpler mechanical manufacturing techniques.

Another aspect of the invention can provide an effective "inert gas" such as steam or _CO2 or HCl vapor to create a curtain of "inert gas" at the end of the nozzle in order to further improve the backward flow from the thermal reaction zone downstream of the nozzle radiation. The present invention provides a design for the annular injection of effective "inert gas" to separate the oxidizing gas emissions from the hot reactor environment, thereby helping to protect the contents of the nozzle from the heat of reaction. The provision of a "inert gas" curtain partially containing the oxygen discharge removes potential combustion from within the nozzle structure, allowing the location of highest temperature to move away from the downstream end face of the nozzle. This protection reduces potential thermal stress on the nozzle tip material and extends the life of the nozzle. Therefore, to avoid direct introduction of the products in the hot reaction chamber into near pure oxygen at the burner face (the condition that produces the highest temperature), it is preferable to place the "moderator" or a part thereof in a surrounding oxygen/fuel jet The form of an annular film is injected into the gasifier. This "inert" layer tends to remove the thermal oxidation zone from the burner face, thereby reducing heat outflow and lowering the temperature achieved at the burner face. _CO2 and steam are preferred effective inert gases due to their ability to absorb infrared radiation.

Another aspect of the design of the present invention provides liquid conduits for distributing or separating halogenated species in order to enable the separate and, if desired, simultaneous (if desired) feeding of different liquid feed streams into the reaction chamber.

The present invention includes feed nozzles used in combination with a gasification reactor for halogenated substances and adapted to be connected thereto. In a preferred embodiment, the nozzle provides a converging-expanding first channel for a gas source of oxygen. The first channel terminates in a discharge orifice at the downstream end of the nozzle. While the first channel may consist of many smaller constituent channels, in preferred embodiments a single channel is considered.

The design of the nozzle provides at least one second passage for the liquid feed stream of the halogenated substance, said second passage terminating in at least one discharge outlet at the downstream end of the nozzle. In some cases, preferred embodiments contemplate providing multiple secondary channels for the addition and simultaneous reaction of different halogenated species. These halogenated species can advantageously be separated before entering the reaction chamber.

The one or more second channels are in fluid communication with a source of liquid halogenated species. The outlet openings of the one or more second channels are preferably designed radially around the outlet openings of the first channels.

A third effective "inert gas" passage is optionally provided. The inert gas is most preferably steam or a major part of it. The third passage (which may be one or more smaller constituent passages) of the inert gas is preferably designed to discharge adjacent to the discharge opening of the second passage.

Channels for inert gas, oxygen source gas, and halogenated species are in fluid communication with appropriate sources of the species. The supply system provides proper temperature and pressure control.

The steam utilized in the "inert gas" channel preferably provides film cooling to the downstream end of the nozzle as well as a "inert gas" curtain that avoids the nozzle end surface from the maximum heat of the gasification reactor in the incipient mixing zone. The steam can also be used as a reactant to provide a source of oxygen and hydrogen. In some embodiments a pilot and/or priming nozzle channel is provided. Alternative designs that can only be scaled down are also disclosed.

The present invention includes a method of feeding a liquid halogenated species to a gasification reactor. The method involves supplying a gas source of oxygen at near sonic or preferably supersonic velocities to orifices of a feed nozzle discharging into a gasification reactor. discharging the halogenated species from at least one discharge port positioned radially around the exiting oxygen source gas so that the oxygen source gas can energize and atomize the halogenated species into the gasification reactor at least downstream of the feed nozzle surface Chamber. The method includes providing water cooling and/or film cooling to the nozzle surface as well as providing a curtain of "inert gas" adjacent to the discharge end of the nozzle to help protect the nozzle surface from the extreme heat of the oxidation reaction. Also provided is a start-up method that utilizes a small volume of feed gas passage and oxygen source gas while slowly increasing the oxygen rate.

The present invention may be better understood when considering the following detailed description of the preferred embodiments when considered in conjunction with the accompanying drawings, in which:

Figure 1 is an explanatory cross-sectional view showing the contracting-expanding channels of the oxygen source gas; it also shows the annular arrangement of the centrally directed nozzle and the circulation outlet end of the halogenated substance; it also shows the channels for inert gas cooling or steam cooling; Also shown is the source of the feed stream and the discharge of the nozzle.

Figure 2 is similar to Figure 1 except that the downstream end of the jacket for the inert gas cooling stream has a different configuration.

FIG. 3 shows the nozzle of FIG. 2 without a centrally directed nozzle.

Figure 4 is similar to Figure 2, but with a separate feed tube for halogenated species.

Figure 5 shows an alternative embodiment of Figure 4 with segmented or separate feed tubes for each halogenated species.

Figure 6 illustrates a nozzle with a cooling medium circuit.

Figures 7 and 8 illustrate the gasification reaction process and gasifier stages in more detail.

Figure 9 illustrates a retractable nozzle which can be adapted to any of the configurations of Figures 1-6.

Figures 7 and 8 show in block diagram form a preferred embodiment of a halogenated species gasification reaction system and suitable for operation of the present invention. Figures 7 and 8 are first discussed to lay the groundwork for the present invention.

The gasification reaction process GPR of Figure 7 converts a feed consisting essentially of halogenated species into one or more useful products. These products may be in the form of useful or marketable acid products 50 and/or product syngas 54 as shown in FIG. 7 . (Alternatively, the reaction products from the partial oxidation reforming step of the process (comprising the same hydrogen chloride, carbon monoxide, and hydrogen components) can be used as feedstock in the synthesis of different useful or marketable products, which are not shown in Figure 7 show.)

Referring now specifically to the production of acid product 50 and/or product synthesis gas 54, as shown in FIG. A plurality of series or parallel partial oxidation reforming reactors (as shown in Figure 8)) supply feed 56, oxygen source 58 and optional moderator stream (not shown) and the required optimal make-up A hydrogen-containing co-feed (not shown) is used to convert substantially all of the halogenated species in the feed to the corresponding hydrogen halides.

The process comprises the steps (illustrated by the preferred embodiment in Figure 7): recovering from the reactor a reaction product stream 60 consisting essentially of one or more hydrogen halides, water, carbon monoxide, and hydrogen, which contains little or no untreated The converted halogenated species are then separated and useful products recovered in quench and particulate removal stage 300 , particle recovery stage 350 , absorber stage 400 , aqueous acid cleanup stage 450 , and syngas polishing stage 700 . Useful products recovered from the reaction products may comprise one or both of a usable or marketable haloacid product and product synthesis gas.

Figure 8 illustrates in more detail the operation of a preferred embodiment of the gasifier stage 200, which shows that an oxygen stream 290, most suitably heated by an oxygen preheater E-290 operated by steam stream 235, is fed as stream 291 to Main burner BL-200. Simultaneously fed to the main combustor is steam stream 298 which is preferably RC1 feed stream 144 and fuel gas stream 296 from preheater E-140 and recycle steam stream 530 from upstream distillation unit T-510. A nitrogen stream 295 is supplied to nitrogen purge the primary gasifier R-200. In a preferred embodiment, the gasifier unit is represented by a primary gasifier R-200 and a secondary gasifier R-210.

The method and device of the invention relate in particular to the feed nozzle BL-200 of the gasification reactor R-200. This nozzle design is useful for atomizing various halogenated species feeds and converting them to higher value products during the reaction. Feeds consisting of mixtures of different halogenated substances (e.g. with chlorinated hydrocarbons, chlorinated fluorocarbons and/or hydrochlorinated fluorocarbons) can be considered for use through this nozzle, which are feeds including liquids and solids . Preferably the nozzle feed consists essentially or completely of liquid. More preferably the feed is substantially free of ash and slagging, the feed comprising less than 5% ash and other inorganic materials, more preferably 1% or less of such materials.

Gasification reactors R-200 and R-210 are preferably under reduced pressure in the form of an oxygen source (preferably in the form of one or more oxygen-containing gases selected from oxygen, air, oxygen-enriched air and carbon dioxide, but more preferably substantially above is oxygen) and optionally supplemented with a hydrogen-containing co-feed capable of converting substantially all of the chlorine in the feed within the reaction product from the partial oxidation reforming reactor zone into hydrogen chloride. Steam is added as a temperature moderator and an additional source of hydrogen in conventional reformer implementations, and steam should be considered as an optional inclusion of other reactants.

Typical burner operating parameters for the nozzle of this design are:

1. Liquid fuel pressure drop: 10 bar (150 psi) at 140 liters per minute (37 gpm).

For a typical liquid orifice, the pressure drop is proportional to the square of the flow rate. Deviations from this relationship indicate possible clogging or coking of the fuel in the nozzle (high differential pressure) or aging of the nozzle tip (low differential pressure).

2. Oxygen pressure drop: The ultrasonic nozzle formed by the pressure ratio is completely different from the pressure drop. The pressure ratio is the ratio of absolute pressure: P _U /P _R . The standard operating ratio of oxygen is 2.75 at 450 kg/hr (10,000 lb/hr). This is the ratio of upstream absolute pressure (P _U ) to gasifier chamber absolute pressure (R _R ).

3. Oxygen temperature: The oxygen temperature of the burner should be maintained at 120°C. Due to the high pressure ratio of the entire burner, the resulting oxygen outlet temperature is close to 25°C. Lower temperatures result in lower velocities, lower atomization efficiency and longer burner vaporization times.

4. Moderator pressure drop: For this low pressure drop gas flow, the pressure drop is actually proportional to the square of the flow. Deviations indicate aging of the annular chamber containing the moderator.

From the discussion above, the operation of the feed nozzle, including the delivery of the feed to the harsh environment, is clearly a critical device. Figure 1 shows a preferred embodiment of a feed nozzle according to the invention in a cross-sectional view. The wall portion R of the gasification reactor surrounding the nozzle N is shown. The downstream nozzle end DSE is indicated as being located in the inner region GR that discharges into the gasification reactor. The DP end represents the radially arranged discharge ports for the feed of the halogenated substance conveyed through the channel HMP. Oxygen source gas flows from an oxygen source 10 (using methods known in the art) through a channel OP into a discharge orifice DO at the discharge end DSE of the feed nozzle N. Figure 1 also shows the flow of effective "inert gas", preferably steam, from the inert gas source 12 to the inert gas channel IGP formed by the nozzle N. The inert gas channel IGP is partly formed by the jacket J1 of the nozzle N. Jacket J1 is preferably represented in the form of an outlet V in the outer wall. Supplementary fuel gas, such as methane, flows from source 13 through nozzle N and partly through fuel gas passage FGP formed by jacket J2.

A passage PP having one or more discharge ports PDP is formed in a pilot nozzle PN located in the middle of the oxygen source gas passage OP. Both the pilot nozzle channel PP and the halogenated substance channel HMP are connected to a source 11 of the halogenated substance. Source 11 is of course a multiple source of halogenated species, and the halogenated species in multiple sources may be the same or different. Supplementary fuel gas is supplied from source 13 to channel PP. Passage PP primarily provides a passage of smaller cross-sectional area for passing the halogenated species feed to one or more atomizing ports PDP. During start-up of the nozzle, both the halogenated substance feed and oxygen are supplied to the nozzle at relatively slow flow rates. Passages PP that provide a smaller volume or cross-sectional area for throughput enable better atomization of the feed material at these initial lower overall flow rates.

Figure 2 differs from Figure 1 in that the jacket J1 which partially forms the inert gas channel IGP does not surround the downstream end DSE of the nozzle N. Jacket J1 contributes to the resulting "inert gas" curtain.

As described more fully below, Fig. 3 differs from Figs. 1 and 2 in that the preferred embodiment does not require the pilot nozzle to be combined to form the pilot passage PP, although this passage PP may also serve as an additional or additional channel through the center of the nozzle. Channel for liquid halogenated substances.

FIG. 4 differs from FIGS. 1-3 in that FIG. 4 specifically shows and provides segmented or separate passages for halogenated species, as indicated by passage HMP1 and passage HMP2 in FIG. 4 . The segmented or separate channels provide passage for the different types of halogenated species while mixing the halogenated species within the gasification reactor at the outlet of the nozzle. In addition, the ring-shaped halogenated substance channel can also be divided to form separate channels.

FIG. 5 shows a related but different embodiment from that described in FIG. 4 . In the design of Figure 4, the segmented or individual material feed channels are located outside channel OP, whereas in the design of Figure 5, the individual feed material channels HMP1 and HMP2 are located within channel OP. Considerations of thermal stability of the feed material and the possibility of feed channel leaks can affect the choice of design between the embodiments of FIGS. 4 and 5 . In the design of Figure 4, the steam surrounds the individual feed channels, whereas in Figure 5 the oxygen source gas surrounds it.

FIG. 6 shows another embodiment in which the wall portion of the nozzle N is cooled with a source of cooling medium, such as water, from a source 14 circulated through a channel WP incorporated into the nozzle N.

As shown in Figures 1-6, in a preferred embodiment of the feed nozzle of the present invention, oxygen or a mixture of oxygen streams flows through a converging-diverging channel terminating in a discharge orifice at the nozzle's discharge. The contraction-expansion part of the nozzle is designed so that the ultrasonic flow of oxygen-containing gas may be obtained at the discharge port. In a preferred embodiment, the halogenated substance, such as liquid RC1, is conveyed through one or more second channels and is discharged into the ultrasonic gas stream from a number of discharge ports around the discharge hole of the oxygen-containing gas. The discharge of the liquefied RC1 is preferably itself radially inwards towards the oxygen discharge stream. As previously mentioned, the feed conduit for liquid RC1 can be subdivided or divided to provide separate feed capabilities for different chemically incompatible RC1's.

For start-up purposes, it is preferred to atomize the feed at a slower initial flow rate using the center-directed nozzle shown in Figures 1, 2, 4 and 6 at the liquid feed spray nozzle discharge (PDP) at the downstream end of the nozzle. This design provides guidance for starting the nozzle at slow feed and oxygen rates, and also makes it loadable for start-up by allowing the reactor to add new incompatible streams.

A separate preheat nozzle (not shown) can be used to heat the gasifier from cool to operating temperature and maintain temperature during short RC1 outages while controlling cooling from hot operating. Due to the large volume of refractory material passing through the gasifier syngas channels, a large amount of heat must be introduced in a controlled manner to heat the refractory material and gasifier chamber to operating temperature prior to the introduction of preferably RC1 liquid. Excessive heating or cooling rates damage the refractory material due to thermal stresses caused by temperature gradients. The function of the preheat burner is very similar to the operation of the primary gasifier and main nozzle or burner as described, except that the fuel is preferably a fuel gas different from the liquid RC1.

For start-up, small intermittent pilots fire preheat burners to heat the refractory. Fuel gas and oxygen are then introduced and mixed externally through a preheat burner. After the flow rate is reduced and a stable flame can be formed, the steam moderator is preferably added in a mass ratio of about 1:1 to the fuel gas. The mass ratio of oxygen to fuel is preferably controlled at about 1.7:1 to 2.0:1 during start-up. It is slightly less than half of the stoichiometric ratio required for complete combustion. The flow rate is slowly increased while maintaining a controlled refractory heating rate at approximately 25°C/hour up to the desired gasifier operating temperature.

As shown in Figures 1-5, in a certain preferred embodiment, the nozzle is an effective "inert gas" preferably added in the form of steam, _CO2 and/or water/halogenated hydrogen vapor around the RC1 and oxygen passages Catheters are provided. Alternatively, the surrounding inert gas conduit may be a conduit for adding methane or another fuel gas as an optional source of additional hydrogen and additional fuel for the reaction process. A selected gaseous process steam stream is added to the reactor to replace or augment steam or methane. The process vapor stream is a non-oxidizing stream containing effective inert gases, RCl or hydrocarbons. Cooling outlets may be utilized in the inert gas channel so that the surface portion of the nozzle is cooled by a thin film of cooling gas formed on the surface. The method of vapor film cooling is shown by Lefebvre (Gas Turbine Combustion - 1983).

The passages of the nozzle (especially the passages of the oxygen source gas and the passages of the halogenated species) are sized to obtain the desired discharge end velocity in conjunction with the expected operating pressure, temperature and steam flow rate. Oxygen is the preferred atomizing gas. Steam provides additional or additional atomizing gas.

In conventional operation, an oxygen source gas such as oxygen and/or steam and/or other oxygen source gas is supplied from source 10 to oxygen source gas channel OP. Liquid halogenated substance is supplied from a source 11 of halogenated substance to passage HMP (or passages HMP1 and HMP2) of halogenated substance. The halogenated substance or fuel gas may also optionally be in fluid communication with the pilot passage PP containing additional or additional feed. The design of the nozzle is such that the oxygen source gas finally reaches the sonic velocity in the divergent part CV of the part of the nozzle wall forming the channel OP. It has been found that the expansion of the oxygen source gas adjacent to the discharge outlet DSE of the nozzle preferably achieves supersonic velocity by means of the expansion portion DV of the nozzle wall portion. Oxygen can sufficiently disperse and atomize the liquid halogenated substance flowing out from the discharge port DP in the halogenated substance passage HMP (or passages HMP1 and HMP2 ) at the supersonic speed. Also, the mixing of the halogenated species such as RC1 with the oxygen source gas such as _O2 should be done just downstream of the nozzle N in the GR region formed in the gasification reactor. Jacket J1 is designed to facilitate effective inert gas (e.g. steam) exiting the inert gas along the portion of the nozzle wall forming the passage for the halogenated material, adjacent to the discharge end of the halogenated material, preferably through or into the exhaust of the halogenated material. outlet, thereby providing an inert gas curtain. The discharge opening DP of the channel HMP for the halogenated substance is advantageously designed so that the halogenated substance can be discharged partially radially inwards towards the axis of the nozzle.

During the start-up of the nozzle, the feed material is initially supplied, preferably to the channel PP, and then flows out of the pilot nozzle tip PT through the discharge port PDP in the pilot nozzle PN, the position and configuration of the pilot nozzle and the discharge port being such that the reactor The gasification reaction begins before the temperature within 200 reaches the process temperature, before the feed reaches its operating flow rate, and before the oxygen source gas in the nozzle reaches sonic velocity. Once the process temperature, pressure and velocity are reached, the pilot nozzle PN is either continuous or disconnected.

Additional fuel gas such as methane can be supplied to the discharge port DSE of the nozzle N through the passage formed by the portion of the jacket J2. Vapor used as an inert gas can be exhausted through outlet V of jacket J1 to help provide film cooling to the wall portion and downstream end portion of nozzle N.

Figure 9 shows a nozzle that can only be reduced. This design is expected to be less efficient than the constriction-expansion design, but is preferred in cases where the oxygen does not reach supersonic velocity. The construction and operation of the shrink-only nozzle design is similar in major respects to the nozzles of Figures 1-6, except that there is no expansion zone.

With regard to the choice of materials of construction for feed nozzles, standard references and literature should be found for appropriate materials of construction in a given environment. Preferably Hastelloy B or C material is used.

The foregoing disclosure and description of the invention are illustrative and explanatory and various changes may be made in size, shape and materials, as well as in details of the illustrated systems, without departing from the spirit of the invention. The invention is claimed using historically speculative terms that describe a single element covering one or more of such elements and two elements covering two or more of such elements.

Claims (25)

1. gasification installation that acts on oxygen and halogenated materials, comprise gasification reactor, and supply nozzle, this supply nozzle has first passage and at least one second channel, wherein first passage contracts earlier and afterwards expands, and end at the tap that is positioned at the nozzle downstream, this tap is used for the oxygen-containing gas discharge is entered gasification reactor, and at least one second channel ends at least one outlet of nozzle downstream, oxygenous body source is communicated with the first passage fluid, and wherein said gas source and described nozzle are suitable near sound wave or ultrasonic velocity oxygen-containing gas is supplied to tap; The fluid supply of halogenated materials and described at least one second channel fluid flow, and an outlet of a wherein said second channel radially is positioned at around the tap of first passage, thereby in use, oxygen-containing gas stream expands and enters, and will be around its liquid gasization of halogenated materials.

2. according to the described device of claim 1, wherein said nozzle provides the third channel of the outlet of at least one its outlet adjacent second passage, and described at least one third channel carries out fluid flow with effective inert gas source.

3. according to the described device of claim 2, wherein said inert gas comprises steam, CO ₂Or nitrogen.

4. according to the described device of claim 1, wherein said nozzle arrangements forms at least one circulation canal, and fluid flow is carried out in described at least one circulation canal and cooling medium source.

5. according to the described device of claim 2, the nozzle arrangements that wherein limits at least one second channel and at least one third channel makes the shared common wall of passage at least in part.

6. according to the described device of claim 3, wherein said nozzle arrangements provides outlet at the outer wall of at least one third channel.

7. according to the described device of claim 1, wherein said nozzle arrangements forms the four-way with outlet at the downstream end of nozzle, and described four-way and gas fuel source are carried out fluid flow.

8. according to the described device of claim 4, wherein said nozzle arrangements makes at least one circulation canal and the shared at least in part common wall of at least one second channel.

9. according to the described device of claim 2, wherein with the outlet structure of at least one third channel and be oriented with the outlet of at least one second channel and combine, so that the third channel outlet passes the outlet of second channel.

10. according to the described device of claim 1, it also comprises at least two second channels, and wherein said at least two second channels carry out fluid flow with independent halogenated materials fluid supply respectively.

11. according to the described nozzle of claim 1, wherein said at least one second channel outlet comprises the ring-type port around the tap that radially is positioned at first passage.

12. according to the described nozzle of claim 1, wherein said at least one second channel comprises that many ring-types are positioned at each first passage tap outlet on every side.

13., wherein described at least one second channel outlet is configured to radially inwardly carry out fluid discharge to small part according to the described device of claim 1.

14. according to the described nozzle of claim 1, wherein said nozzle arrangements also provides the directional nozzle that is positioned at first passage element, described directional nozzle element ends at tap at the downstream end of nozzle, and this directional nozzle element and gas fuel source are carried out fluid flow.

15. one kind is fed to halogenated materials according to the method in the described gasification reactor of claim 1, this method comprises the oxygen source gas near sound wave or ultrasonic velocity is fed to the tap that enters the feed nozzle in the gasification reactor; The liquid halogenated materials is discharged from the outlet that at least one radially is positioned at around the oxygen source gas of discharge, thereby diffuse into and atomized liquid halogenated materials in gasification reactor at the external oxygen source gas of feed nozzle at least.

16. in accordance with the method for claim 15, it comprises the discharge of the contiguous halogenated materials of effective inert gas is discharged.

Comprise exhaust steam 17. in accordance with the method for claim 16, wherein discharge effective inert gas.

18. in accordance with the method for claim 15, it cooling medium that comprises that utilization circulates in nozzle passage cools off the outlet side of feed nozzle at least.

19. in accordance with the method for claim 16, it comprise effective inert gas through qualification the halogenated materials passage to small part wall and the inert gas film that on wall, forms.

20. in accordance with the method for claim 17, it comprises from being limited to the outer wall that small part ground forms the inert gas passage and discharges effective inert gas.

21. in accordance with the method for claim 15, it comprises the downstream end of postcombustion gas at nozzle is drained in the gasification reactor.

22. in accordance with the method for claim 16, it comprises effective inert gas is discharged at the effluent stream that the downstream end of nozzle passes halogenated materials.

23. in accordance with the method for claim 15, its outlet side that is included in nozzle is discharged at least two kinds of halogenated materials respectively.

24. a starting is according to the method for the gasification reactor of the described halogenated materials of claim 1, this method is included in the tap supply oxygen source gas of the feed nozzle that enters gasification reactor; Downstream end at nozzle in the oxygen source gas of discharging is discharged the fuel gas logistics; Speed with oxygen source gas in nozzle is increased to SVEL.

25. in accordance with the method for claim 24, it comprises when oxygen source gas during near SVEL, little by little discharges the liquid halogenated materials from least one outlet that radially is positioned at around the oxygen source gas of discharge.

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