CN1427879A - Refractory pressure vessel - Google Patents

Abstract

A reactor for gasifying carbonaceous materials including an interior lining of one or more refractory materials, a pressure vessel enclosing the refractory lining, preferably a corrosion resistant cladding lining the pressure vessel and one or more channels for circulating a heat transfer fluid substantially jacketing the pressure vessel to control pressure vessel wall temperature and preferably also lining temperature during down time.

Description

Fire-resistant pressure vessel

technical field

The invention relates to a refractory container for gasifying carbonaceous materials, in particular to a container wall structure and a temperature control system.

Background technique

Related inventions include a prior patent application entitled Method and Apparatus for the Production of One or More Useful Products from Less Valuable Halides, PCT International Application PCT/US/98/26298, disclosing Dated July 1, 1999, International Publication No. WO99/32937. This PCT application discloses a method and apparatus by which, via a local oxidative reformulation step in a gasification reaction vessel, it is possible to achieve a process that will substantially contain halides, especially by-products obtained through a series of chemical manufacturing processes, as well as waste chlorine Convert hydrocarbons to one or more "higher value products".

In this regard, gasification is a well-known technique for consuming by-products and useless carbonaceous materials, and producing useful higher value products therefrom. The related application referred to in the preceding paragraph provides a new method for the treatment of special grades of carbonaceous materials and wastes that are currently processed primarily in liquid thermal oxidation facilities, namely halides and Especially by-products and unwanted chlorinated hydrocarbons. The refractory pressure vessel of the present invention is particularly useful in handling the special grades of carbonaceous materials described above, but is also useful in gasifying other carbonaceous materials.

Gasification offers many potential advantages for thermal oxidation of liquids, including lower economic costs, less emissions, and the acquisition of maximum chemical value for the feed components. With regard to the treatment of halogenated carbonaceous materials, gasification is also a more applicable technology than other halide waste treatment technologies (i.e. in addition to liquid thermal oxidation technology), in that gasification can be applied to a wider Wide range of feed components.

In the following, an embodiment of the gasification process of halides will be discussed in conjunction with the block flow diagram shown in FIG. 1 . Within the gasification process, gasification mainly occurs under partial oxidation conditions, ie, a sub-stoichiometric ratio of oxygen to fuel with an excess of hydrogen. The reaction temperature is higher than 1200°C, usually higher than 1400°C, and the reaction pressure is about 5 bar (barg). Under these conditions, the halides in the halogenated organic material should be converted to their gaseous hydrogen halide forms.

In general, halides are corrosive both in the gas phase and in the condensed liquid phase. The dry vapor phase corrosion rate of most materials in structures in contact with hydrogen halides increases exponentially with increasing temperature. The corrosion rate of aqueous hydrogen halides to materials in contact with them also increases with increasing temperature, but the corrosion rate is intensified when oxygen or oxidized metal salts are present. The corrosiveness of hydrogen halide requires more attention when designing a safe and reliable pressure vessel used as a gasification reaction vessel.

In the field of gasification of hydrocarbons other than halogen-containing feedstocks, two main refractory vessel designs are used. As shown in Figure 3, a "hot wall" design has one or more layers of refractory material, namely the hot face 20, insulating refractory layer 22, ceramic fiber paper 24 and optionally castable or plastic refractory layer 26 , the refractory layer 26 just limits the transfer of heat from the reactor chamber C to the outer side of the container wall 28, which can be a carbon steel shell, polytetrafluoroethylene or a hydrochloric acid-resistant nickel-based alloy B-2 (ID) lining, and ultimately limit Heat is lost to atmosphere A. This design by itself does not provide an active means of controlling the temperature of the vessel walls. This results in large variations in vessel wall temperature as a function of operating conditions, integrity of the refractory, and environmental conditions. An aspect of the present invention is to improve upon this design, which was found to be suboptimal for gasifying halogenated organic materials, primarily because of the lack of active wall temperature control and the effect of hydrogen halide imparted by such control on Corrosion of container walls.

A second design of a refractory wall structure for hydrocarbon gasification, an inner "membrane wall" design, is shown in FIG. 4 . The inner “membrane wall” design here provides one or more layers of refractory material 20 , 22 , 24 and an optional 26 within a so-called membrane 34 arranged in the pressure vessel 28 . The membrane is formed by any number of conduits or channels 38 (typically pipes) for circulating a fluid thermal control substance 36 . Together the catheters make up the inner "membrane" scaffold. Both the membrane and the refractory are contained within a pressure vessel (leaving a small space between the membrane and the vessel wall). Membranes can be made from any material of construction. A heat transfer fluid flows through the membrane conduit to absorb heat from the reactor chamber C, thereby limiting the vessel wall temperature. Inner membrane systems that do provide a control over the vessel wall have other disadvantages such as high constructional costs and high maintenance costs in harsh environments. The inner membrane design can be further complicated to reduce gas leakage to the pressure vessel wall if a "gas tight" design is desired. One aspect of the present invention is to improve the design of the inner membrane used on reactors for the gasification of carbonaceous materials, especially halides, thereby producing hydrogen halides. Inner membrane designs are too complex and expensive to construct and maintain, the latter being very dangerous especially in harsh hydrogen halide gasification environments.

Jacket cooling techniques are well known. For example in R.E.Markovitz, "picking the bestvessel jacket", Chem.Engr.pp 156-162, Nov.15, 1971; R.E.Markovitz, Chapter: Heat transfer: Jacketed Vessels In Heat Transfer Design Methods, ed. JJ Mcketta, Marcel Dekker , 1991; W.R.Penney, Section 3.14 (3.14.1, .2 and .3) In: Hemisphere Handbook of Heat Exchanger Design, G.F.Hewitt, ed.1981; I.H.Lehrer, "Jacket-Side Nusselt Number", IEC Proc.Des . Dev., 9 No. 4, pp 553-558, 1970; J.A. Kaferle, Jr. "Calculating Pressures for Dimple Jackets", Chem. Engr., pp 86, November 24, 1975. However, a traditional application of jacketed reactors is to control heat transfer to and from the reactor itself (usually a liquid phase reactor) in order to control the reaction temperature or the temperature of the reactor contents. In contrast to the above, the present invention is designed to provide a jacketed reactor for the gasification of carbonaceous materials and especially halides. The temperature-controllable jacketed gasification reactor of the present invention is not used to control the average temperature of the contents of the reactor, but to control and limit the temperature of the pressure vessel wall and cladding. If the above jacket design is used, the reaction chamber and The temperature of its contents itself is essentially below normal operating levels.

Thus, current gasification mainly uses "hot walls" with suitable materials or linings for use in corrosive conditions, or an inner "membrane wall" that prevents heat from passing through the refractory The system reaches the pressure vessel wall, however the present invention takes a number of unique ways to enable the present invention to function as both the "hot wall" and the inner "membrane wall" described above. The novel jacketed reactor designed by the present invention has a heat transfer fluid circuit for wall temperature control which includes cooling during operation and heating during standstill. The wall temperature control system limits the maximum or high wall temperature, thereby limiting corrosion by hot lean gases. Because high levels of hydrogen halide are expected during processing according to the above-referenced PCT application, and because the vapor phase corrosion rate of materials such as HCl increases dramatically with temperature, tight wall temperature control is very important. important.

Reasons for higher wall temperatures are high ambient temperatures, high internal gasifier operating temperatures, or gas permeation or "bypassing" through the refractory material so that the gas contacts the vessel wall. These "hot spots" are not uncommon in large refractory lined vessels. Therefore, as mentioned above, a simple hot wall design is not advisable for long-term servicing of gasifiers. In addition, wall temperature control is extremely important for gasifiers, especially for gasifiers that vaporize halides, during setup, start-up, warm-up, (temperature) drop or shutdown. The wall temperature control of the present invention is preferably designed to prevent condensation of cold or wet aqueous acids, especially hydrogen halides. Aqueous acids or hydrogen halides are very corrosive. Preventing the occurrence of such condensation is critical to optimal corrosion control of most materials in a structure. When using prior art hot wall or inner membrane systems, these "cold" conditions can occur at local cold spots where there is a large amount of heat loss (eg, at burners, pressure vessel heads) because the surrounding environment is cold, precipitating. Thus, tight wall temperature control is also important to prevent condensation of wet aqueous hydrogen halide and the associated corrosion.

The novel jacketed vessel construction of the present invention also eliminates the cracks and pressure points present in the membrane designs described above. Membrane designs are mainly realized with curved and welded pipes or channels. This bending and welding process inevitably leads to the existence of residual material stress and some cracks. These higher pressure areas and fractures lead to higher localized corrosion rates present in the membrane material. A fire-resistant pressure vessel with an outer jacket for temperature control provides a simpler, less expensive construction and maintenance procedure than an inner-membrane design. Intimal walls require many plate or component parts to be incorporated into the pressure vessel. To facilitate future maintenance, the above-mentioned components are made small enough to pass through manholes provided in the container. The above components must be assembled into the container. Thus, the inner membrane design is complex, requiring a certain strength to support the weight of all refractory materials, and complex in allowing thermal growth differences between the refractory material, membrane wall, and pressure vessel shell. A relatively uniform wall temperature can be obtained by the outer temperature-controllable jacket container, so that the above-mentioned difference in thermal growth can be reduced.

In addition, the number of pressure vessel perforations is limited in an external temperature-controlled jacketed reactor design compared to an inner membrane wall design. The inner membrane wall requires multiple nozzles for coolant inlets and inlets. These vessel wall perforations present undesirable pressure points and crevice corrosion to the pressure vessel. In contrast, pressure vessels with a smooth and simple internal shape combined with an external temperature-controlled jacket can be clad, coated, and lined with a variety of materials simply and economically.

In addition, because the external temperature-controlled jacket design system can make the exposed surface temperature of the vessel more uniform (which can obtain better corrosion control), so the external temperature-controlled jacket reactor design can reduce inert gas purge necessary. However, the aforementioned inert gas flushing of the gas space or chamber behind the intimal wall is necessary. The gas dilution from these purges is undesirable.

Contents of the invention

The invention includes a gasifier for gasifying carbonaceous materials, especially halides. The reactor includes an inner liner of one or more refractory materials defining a reactor vessel chamber, a pressure vessel surrounding the refractory lining and the reactor chamber, and a closed One or more channels in the reactor cavity through which the heat transfer fluid is circulated. The one or more channels are connected to a heat transfer fluid circulation system. Thus, pressure vessel and liner wall temperature can be controlled. In practice, when the temperature of the reactor chamber is high, a circulation system is operated to cool the vessel wall, or to maintain the vessel wall temperature below a certain ideal value. When the reactor is not operating, the circulation system is operated to heat the reactor chamber lining above the minimum desired temperature. Most preferably, the present invention includes a corrosion resistant cladding liner.

The present invention includes a method for gasifying carbonaceous feedstocks, including halides, in a reactor comprising a first pressure vessel lined with a refractory material, the method comprising the steps of: A carbonaceous feedstock and oxygen are supplied to the reactor to produce products therefrom including synthesis gas; a heat transfer fluid is circulated to contact the outside of the first pressure vessel wall portion so that the fluid acts to move the outside The reactor wall temperature is controlled above the temperature on the outside of at least the first pressure vessel wall portion (the temperature is lower than the target level), which is substantially lower than the operating temperature of the reactor and is preferably about 150° C. to 250° C. ℃.

The preferred embodiments of the present invention will be described in detail below in conjunction with the accompanying drawings, so as to help better understand the present invention.

Description of drawings

Fig. 1 is the flow chart of the preferred embodiment of applying the gasification process of the present invention;

Figure 2A details specific features of the gasifier in Figure 1;

Figure 2B shows a heat transfer fluid control system for use with the gasifier of Figure 2;

Figure 3 shows the prior art hot wall concept for a reactor vessel;

Fig. 4 shows the concept of the film type water-cooled wall reactor vessel used in the gasifier in the prior art;

Figures 5A-5F illustrate an integrally jacketed container and "container-in-a-container" concept of the present invention having one or more channels defined by various components, including recesses and partitions;

Figures 6A-6D illustrate an outer membrane water wall or plate embodiment of the present invention having channels defined by coiled structures;

Figure 7 shows the arrangement of the sleeve area.

Detailed ways

Since the following examples are the original application of the present invention, the following reference is made to our related PCT application (Title of Invention: Method and Apparatus for Producing One or More Useful Products from Less Valuable Halides, PCT International Application PCT/US/98/26298, Publication Date: July 1, 1999, International Publication No. WO99/32937) An example of the best illustrative gasification process for halides is briefly described discuss. This gasification process can be viewed as comprising several main processing zones, as shown in the block flow diagram of Figure 1, where,

1) Vaporizer 200

2) Quenching 300

3) Particle removal and recovery 350

4) Recovery and cleaning of aqueous HCl 400, 450

5) Syngas completed 700

For the convenience of the following description, the hydrogen halide produced is assumed to be HCl.

The gasifier zone 200 in the preferred embodiment shown in Figures 2A and 2B consists of two reaction vessels R-200, R-210 and auxiliary equipment mainly for reforming halides (mainly RCl's). In this example, the halogen-containing feed (stream 144 ) is atomized into primary reactor R-200 along with oxygen 291 and gas stream 298 . In the harsh gasification environment, RCl and other components are partially atomized and converted into carbon monoxide, hydrogen chloride, hydrogen, a small amount of water vapor and carbon dioxide, and a small amount of other substances such as soot (mainly carbon). The product from R-200 preferably flows into a second reaction vessel R-210 where all reactions are completed, thus efficiently producing all halogenated species while reducing unwanted by-products Such as soot.

Since hydrogen halides or HCl are corrosive both as hot lean gases and as condensate, the reactor housing and connecting lines are preferably jacketed, as will be explained more fully below in accordance with the invention. The placement of the jacket creates one or more passages connected to a closed heat transfer fluid system S-280, partially shown in FIG. 2B.

Continuing with the gasification system shown in the block flow diagram of FIG. 1, the hot gas from R-210 is preferably cooled at quench zone 300 by direct contact with the circulating water flow. Reactor effluent or product gas and the water stream can be mixed directly in a quench vessel. The mixture then flows into a gas-liquid separator drum from which the quenched gas exits the upper part and the bottom liquid can be cooled and recycled to the quench zone.

Particulates (eg, including soot, etc.) in the product gas exiting the reactor system can be separated from the gas stream by scrubbing in the scrubber of the particulate recovery step 350 . The gas stream from the scrubber is then preferably introduced into a hydrogen halide or HCl absorption column 400. The non-condensable components flow through the upper portion of the absorber and continue to the syngas completion zone 700 . HCl in the gas exiting the scrubber can be absorbed to provide an aqueous acid stream from the bottom. The aqueous acid stream is filtered and passed through an acid purification unit 450 to remove the last remaining particulates and organics to produce a grade of aqueous HCl product. This product can be sold as desired or further processed to produce anhydrous HCl (suitable steps and apparatus required for this processing have been disclosed in previous applications). The synthesis gas finishing zone 700 includes an alkali scrubber and a synthesis gas waste gas treatment system.

Having described an example of a halide gasification process, we now return to look in detail at the gasifier 200 shown in FIG. 2 . The gasifier zone 200 in the above example consists of two reaction vessels R-200, R-210 and auxiliary equipment mainly for reforming the halogen-containing feed. For ease of illustration, the halogenated feed is assumed to include chlorine-containing organic species.

The main gasifier R-200 in the preferred embodiment shown is used as a down jet stirred reactor whose main function is to atomize the liquid fed to the R-200 and to evaporate the liquid, and generally The evaporated liquid is carefully mixed with oxygen, moderator, and thermal reaction products. The gasifier works best at a temperature of 1450°C and a pressure of 5 bar (75 psig). These stringent conditions ensure that all feed components fed to R-200 are nearly completely converted.

In order to prevent the gasifier shell of the above embodiment from being corroded by hot dry hydrogen halide or aqueous hydrogen halide condensate, the present invention discloses a gasifier shell provided with a jacket to facilitate pressure vessel wall temperature control.

A portion of the jacket system is shown in Figure 2B, wherein the system provides circulation of a heat transfer fluid into one or more channels defined by the jacket to facilitate wall temperature control. The system S-280 includes a cooler E-280, collection drum D-280, and a plurality of pumps P-280 for circulating heat transfer fluid, wherein the heat transfer fluid is preferably Dowtherm GRP (Dowtherm GRP ) or syltherm 800, but can also be other fluids including water. Hot refractory-lined gas containers, pumping piping, and quench inlets are preferably fully jacketed. During normal operation, under the cooling effect of the heat transfer fluid from the fluid control system S-280, the gasification process chamber is transferred to the vessel shell and pipeline (mainly stainless steel shell) through the refractory material lining. heat. A small heater E-281 is also preferably provided for heating the heat transfer fluid from cold start to working condition and for maintaining the temperature of the lining during shutdown.

The temperature of the container shell is preferably controlled at about 200°C, or between 250°C and 150°C. The theoretical dew point temperature of hydrogen halide containing gas mixture is about 130-150°C. However, the actual dew point temperature is changed by the addition of salt, metal or other corrosive substances. Thus, the wall temperature is preferably maintained at a safe margin above the above-mentioned theoretical dew point temperature. When the temperature is higher than 200 °C, the corrosion rate of dry gaseous HCl increases exponentially with temperature. Thus, there is no need to heat the vessel shell walls excessively beyond that required to prevent water condensation. In a preferred embodiment of the running system, the jacket system can control the wall temperature at all times (even during downtime) except when system maintenance is required. Even during downtime, this control prevents atmospheric moisture from condensing into corrosive liquids due to the presence of residual HCl, etc. in the system.

As mentioned above, because of the potentially enormous corrosiveness of the high temperature gas mixture and condensate, it is desirable to have a constant control of the reactor wall temperature. In order to stabilize and tightly control the reactor wall temperature below the extreme temperatures of the gasification reactor, the present invention discloses a pressure vessel lined with a refractory material, preferably carefully selected to ensure that the gasification The life of the carburetor is longer.

As mentioned above, the "hot wall" concept in the prior art as shown in Figure 3 is not optimal and cannot control the pressure vessel wall suitable for gasification of carbonaceous materials (especially chlorine-containing materials) by itself. condition. With the "hot wall" concept of the prior art, the wall temperature cannot maintain sufficient requirements including temperatures above the dew point temperature and below the ideal maximum non-humidity temperature at all times and within the necessary range of environmental conditions. For example, outgassing of refractories 20, 22, 24 and optionally 26 or a localized refractory failure can cause wall 28 to overheat resulting in a greater corrosion rate. Additionally, wall conditions cannot be controlled during start-up, shutdown, shutdown, and normal operation in cold ambient conditions. For a vessel operating at 5 bar pressure, especially if it contains hot HCl carrying syngas, this situation and the presence of hazards are very bad.

As mentioned above, the prior art inner membrane design shown in Figure 4 is better than the "hot wall" shown in Figure 3 in terms of wall temperature control, but still not ideal. The structure of the membrane 34 is complex and requires multiple panels and sections to cover the entire container 28 area, presenting a design and manufacturing challenge. Membrane 34 also presents mainly maintenance issues such as the need to access the vessel, remove the refractory and possibly remove the membrane. Since the membrane must be of a high-alloy material, this design requires more outlay than the design of the device housing according to the invention. The vessel 28 requires a liner or cladding 30 or a complex cavity gasket system with an inert gasket gas. This litter (mainly _N2 ) is an undesirable gas diluent. In some designs of the invention, no such coating is provided.

The jacketed housing of the present invention comprising one or more outer channels as shown in Figures 5-11 is combined with the heat transfer fluid control system shown in Figure 2B. The jacketed shell is the optimum design for vaporizer vessels, especially those that vaporize halides. This design has a good level of wall temperature control, reliability and cost efficiency. The wall temperature of the vessel in the present invention can also be maintained above the dew point temperature in substantially all modes of operation. Even in the case of gas bypass or failure of local refractory materials 20 and 22, the heat transfer design of the above-mentioned device housing has efficient, practical and regular cooling capacity to limit the wall temperature.

Other designs of jackets as shown in Figures 5-11 include inner jackets, outer membrane walls or plates, welded "half-pipes", dimpled jackets, spiral jackets for containers, and outer panels. Jacket cooling can be accomplished by a variety of techniques. The temperature-controlled jacket cooling is a "vessel-in-vessel" design, as shown in Figure 5 and Figure 2A. The heat transfer fluid 36 is circulated through one or more channels 38 defined by such jacket 40, wherein the channel may only include the space between two container walls. In this space, as shown in Figure 5B, the heated temperature control fluid is introduced, preferably using a nozzle in a random orientation, to create a swirling flow throughout the jacket. The structure of flat jacket cooling is the simplest, so its initial cost is also low. The flat sleeve cooling is more suitable for condensing and heating media, but not suitable for sensitive fluids. One reason for this is that larger channels lead to lower flow velocities and correspondingly lower heat transfer efficiencies, where the magnitude of the efficiencies is largely determined by the conditions of natural convection. Ordinary jacket cooling is actually adding double walls to the reaction vessel. In particular, if sensitive fluid heating or cooling is set in common jacket cooling, it is recommended to use a stirring nozzle as shown in Figure 5B. Agitation nozzles 50 may be used to direct more or less tangentially of feed liquid 36 into jacket 40 while increasing effective flow velocity and turbulence levels. Then to be used in condensing media, impact protection is highly recommended. In addition, larger or more filling nozzles can also be used.

A "sleeve-in-sleeve" design with internal partitions as shown in Figures 5C and 5D is preferred. Therein, heat transfer fluid is circulated through a chamber defined by two pressure vessel walls (inner pressure vessel wall 28 and outer pressure vessel wall 40 ) and a plurality of partitions 52 . The circulation of the fluid is controlled by the circulation control system to strictly control the flow rate and heat transfer efficiency of the heat transfer fluid, so as to keep the temperature of the container wall and the coating within a certain range, which is basically not affected by the temperature in the reactor. Optimal conduit design balances the relationship between heat transfer coefficient and pressure drop. In a preferred embodiment, the preferred separator is wound around the reactor shell 28 in a helical fashion.

Typically, helical plate diaphragms consist of a helical band welded along the pressure vessel shell. This allows the fluid in the jacket to flow around the container in smaller channels. There is naturally some gap between the edge of the bulkhead and the inside of the casing through which a portion of the circulating fluid can pass. Otherwise, the jacket can be viewed much like a coil.

The dimpled jacket shown in Figures 5E, 5F is another design of the jacket with a baffle. As shown in Figures 5E and 5F, the housing 40 is provided with regular recesses 54 made of the same material as the housing. These recesses 52 are of regular form and serve to induce turbulence. These recesses 52 are welded to the container wall 28 .

Another jacket cooling technique may use a membrane wall, "half-pipe" jacket, or plate-screw approach as shown in Figures 6A-6D. For the half-pipe design shown in Figures 6B, 6C, a plurality of half-pipe conduits 56 are welded to the vessel shell 28 to provide parallel channels 38 for the heat transfer fluid 36 flow. An inlet and outlet 58 are provided to circulate the heat transfer fluid 36 . The thermal control coil 260 shown in FIG. 6A for use in the endomembrane system can also be used as the outer casing 40 . Half-pipe casings basically consist of a pipe cut longitudinally which is then welded to the shell. This design is suitable where high jacket pressures are required, but the method is expensive because two long welds along each side of the cut pipe are required. Since the geometry is known and no bypass is possible, the heat transfer is well defined. Half-pipe jackets are more suitable for sensitive fluids such as water or other similar heat transfer fluids.

It could also be a welded flat coil as shown in Figure 6D, with protrusions to allow for relatively good fluid passage. It is also possible to provide a splint on the flat coil which is clamped to the container rather than welded to it.

As shown in Figure 7, the housing can be divided into several sections, each section having independent inlets and outlets. In some demanding occasions, the setting of these areas is conducive to improving the uniformity of temperature in the container so that when using condensing medium, the condensate can be quickly removed from all areas of the jacket, and in addition, it can reduce the temperature change in sensitive media. Control the welding temperature in any vapor space area and keep the pressure drop in the jacket to the allowable value.

According to the invention it is desirable to cover the walls of the pressure vessel. Non-metallic cladding designs are not ideal for vaporizer vessels because non-metals are not "tough" enough for long life. Uncontrolled thermal movement and localized hot spots due to refractory failure or gas bypass have the potential to compromise the integrity of prior known non-metallic linings. Therefore, in the preferred embodiment of the present invention, a high alloy corrosion resistant metal cladding 30 is preferably used.

As mentioned above, in actual operation, the temperature of the inner part of the container wall is preferably kept at or slightly higher than 200°C to ensure that it is higher than the dew point temperature. The dew point temperature of most HCl gases is estimated to be in the range of 130-150 °C, but the local dew point temperature increase caused by the addition of metal corrosion products makes the operating temperature higher. Based on the above considerations, a higher temperature synthetic heat transfer fluid (such as Dowtherm A) is used in the circulation path 38. High temperature stability of the fluid is important to reduce the effect of hot spots on long-term fluid stability and temperature control. Fluid properties and case failure conditions should dictate the jacket system operating pressure.

Care should be taken to maintain the gasification pressure vessel contents, nozzle design and fittings. The shell penetration should be minimal, the necessary penetration should be provided with an outer jacket and be designed for temperature control.

The jacketed reactor design of the present invention as shown in Figures 5-11 utilizes one or more inner layers of refractory material 20, 22, 24 and an optional layer 26 adapted to be exposed to hot feed gas that The gas may be a gas containing hydrogen chloride, see Figure 5A. The one or more layers of inner refractory described above primarily include a "hot side" refractory layer 20 for chemical resistance and an insulating refractory layer 22 for heat transfer control. High alumina refractory bricks (greater than 99%) with insulating refractory bricks are an option. This refractory system is located directly within the pressure vessel 28 . An outer insulating layer 32 may also be included. If desired, any amount of corrosion resistant material may be surrounded as a cladding around the layer of refractory material to protect the pressure vessel wall from corrosion by the corrosive medium. For example, the container wall shell can be provided with a lining or other coating of plastic material, ceramic, glass. Optimally, however, the vessel walls are clad with a corrosion resistant Alloy 30 metal. This alloy has the best corrosion resistance and mechanical strength. Other known liners can often suffer from damage and gassing due to thermal movement of the refractory material or differential expansion rates between the liner and the stainless steel shell. Nickel Alloy B3 and Alloy C-276 are two good coatings to replace the lining. Each has good corrosion resistance to dry hydrogen chloride as well as aqueous hydrogen chloride solutions. Hydrochloride-resistant nickel-based alloy C-276 has little corrosion resistance to pure aqueous hydrogen chloride solution, but has high corrosion resistance to solutions containing small impurities such as metal salts and dissolved oxygen. The use of a corrosion resistant alloy layer also allows the use of low alloy stainless steel in the actual pressure vessel shell 28 construction.

One or more passages provided by an external jacket cooling system 40, and then separately and independently (within a limit value, that is, a given reactor temperature range) control the temperature of the pressure vessel 28 and the lining, so that Corrosion resistance and container integrity of the present invention. In this way, the temperature of the pressure vessel and lining can be maintained above the condensation temperature of the vessel contents, plus a normal safety margin (50°C). Ensuring such temperature control also facilitates cladding material selection for maximum dry gas phase corrosion resistance.

As mentioned above, in the present invention, vessel wall temperature control is achieved by means of a "jacket cooled" vessel, that is, the vessel is provided with one or more conduits 38 and the temperature control medium 36 is passed through said conduits. As shown in Figure 2B, the catheter should be connected to the fluid circulation control system.

Preferred embodiments of the present invention may utilize one-stage or two-stage heat transfer. Two-stage systems require a more complex design and piping system, but have a higher heat transfer coefficient. The optimal design, as shown in Figures 2A and 2B, utilizes a simple one-stage heat transfer fluid. The heat transfer fluid can be water or other commercially available fluids such as Dowthern ^(R) products or Therminol ^(R) products, among others. Important parameters to consider when selecting a fluid relate to the physical properties and performance of the fluid and its interaction with the jacket design. These properties include operating temperature, maximum temperature, minimum operating temperature, viscosity, density, vapor pressure, surface tension, thermal conductivity, fouling characteristics, and degradation products. A number of factors for selecting a heat transfer fluid are discussed in "Sizing Heat Transfer Fluids and Heaters," by G.E. Guffey II, Chemical Engineering, October 1997.

A preferred embodiment of the heat transfer fluid circulation system S-280 of the present invention comprises an intermediate drum or tank D-280 for maintaining the total volume of fluid, a pump P adapted to pump the liquid into the network and jacket -280, and a heat exchanger H-280, the function of which is to: (1) transfer heat to the atmosphere or other medium under normal operating conditions; (2) heat the heat transfer fluid to of organic material prior to bringing the system into operating conditions. The system S-280 is equipped with suitable means (not shown) to control the jacketed reactor surface temperature at a desired value which reflects the conditions in a typical gasification reactor process.

For ease of understanding the design of the present invention, give an example as follows:

example 1

The following feed streams are supplied to the gasifier through a suitable mixing nozzle:

Chlorine-containing organic materials: 9037kg/hr

Oxygen (99.5% purity): 4419kg/hr

Recovered steam or moderator: 4540kg/hr

[58.8 wt% water vapor, 41.2 wt% hydrogen chloride]

Such a gasification reaction produces a hydrogen chloride-enriched synthesis gas stream and chamber conditions at a temperature of about 1450° C. and a pressure of 5 bar. In this example, the reactor is equipped with 6" (1524cm) thick hot-faced high-alumina refractory bricks, and the brick is covered with 9" (22.86cm) thick insulating refractory bricks. This refractory mounting design prevents heat loss to the vessel wall. The pressure vessel is a low alloy stainless steel cladding of 3mm thick nickel base alloy C-276. The container includes an integral jacket covering substantially all of the surface of the container. The jacket includes internal baffles to direct the fluid flow and control the flow rate and heat transfer coefficient. A typical limit is a minimum of 1 m/sec to reduce fouling and maintain an acceptable heat transfer coefficient. A maximum velocity of 4m/sec limits the pressure drop to an acceptable range. The heat transfer fluid is stored in a low pressure altar. The altar can be filled with inert gas to control pressure and exclude oxygen from the system. A typical flow rate of 1200 gpm of fluid is pumped through the jacket cooling system by a centrifugal pump. Fluid returning from the jacket passes through a water-cooled heat exchanger to remove heat from the system. The heat exchanger outlet temperature was controlled at 200°C, which was about 50°C higher than the pure hypothetical condensation temperature of the fluid in the vessel. The 50°C is a safe value to avoid the influence of impurities that raise the condensation temperature. In this way, the surface temperature is controlled at about 200°C.

The above descriptions and disclosures of the present invention are only for explanatory purposes, and various changes may be made to the dimensions, shapes, materials and other details of the above system without departing from the spirit of the present invention. The invention is defined using terms that depend on a historical assumption that a part contains one or more of such parts and that two parts contain two or more of the specified parts.

Claims (25)

1. reactor that is used for gasification materiel, this reactor comprises:

The liner of making by one or more refractory materialss;

First pressurized vessel that surrounds refractory liner; And

The passage of one or more heat-transfer fluids that are used to circulate, these one or more passages basically shell type cool off this first pressurized vessel the outside at least a portion and link to each other with this heat-transfer fluid recycle system, its this heat-transfer fluid recycle system is used to remove heat so that vessel wall temperature is limited under the temperature of reactor.

2. reactor as claimed in claim 1, wherein these one or more passages load onto cover for basically the whole refractory liner of this first pressurized vessel.

3. reactor as claimed in claim 2, wherein this recycle system is used to increase heat.

4. reactor as claimed in claim 3, wherein the recycle system and these one or more passages combine with reactor and make to be lower than a maximum target runtime value in reactor run duration control pressure vessel wall temperature, increase liner temperatures between the down-time period at reactor simultaneously and are higher than a minimum target value.

5. reactor as claimed in claim 1, wherein pressurized vessel includes one deck corrosion resistant lining.

6. reactor as claimed in claim 1 wherein is provided with insulation layer in the outside of these one or more passages.

7. reactor as claimed in claim 1, wherein these one or more refractory materialss comprise the hot side refractory materials that is positioned at the refractory materials inboard.

8. reactor as claimed in claim 5, wherein corrosion resistant lining comprises the noncorroding metal alloy.

9. reactor as claimed in claim 5, wherein corrosion resistant lining comprises non-metallic liner.

10. reactor as claimed in claim 1, wherein this one or more passages to small part is limited by second pressurized vessel that surrounds first pressurized vessel.

11. reactor as claimed in claim 10 is comprising the dividing plate between second pressurized vessel of this first pressurized vessel.

12. reactor as claimed in claim 2, wherein this one or more passages to small part is limited by first pressurized vessel that surrounds second pressurized vessel.

13. reactor as claimed in claim 12 is comprising the dividing plate between second pressurized vessel of this first pressurized vessel.

14. reactor as claimed in claim 2, wherein shell type these one or more passages of cooling off this first pressurized vessel are formed by screwed pipe, and this screwed pipe forms the overcoat of the part of the outside surface that covers first pressurized vessel basically.

15. reactor as claimed in claim 1, wherein reactor comprises that one is suitable for that liquid halide is transported to feed nozzle in the reactor and one and is suitable for gas from reactor expellant gas delivery port.

16. reactor as claimed in claim 1, wherein these one or more refractory materialss comprise that one is suitable in the face of being at least the hot side material of 1550 ℃ temperature of reactor.

17. a method that is used for comprising in the reactor gasification carbon-containing feeding of halogenide, this reactor comprises that has refractory-lined first pressurized vessel, and this method comprises the steps:

Under reductive condition, carbon-containing feeding and oxygen are fed in the reactor so that therefrom produce the product that comprises synthetic gas;

The heat-transfer fluid circulation to contact the outside of the first pressurized vessel wall part, like this, is being exceeded 150 ℃～250 ℃ at least with outer reactor wall temperature control under the fluid effect than the temperature on the outside of the first pressurized vessel wall part.

18. method as claimed in claim 17 is comprising the operating temperature in the reactor vessel is maintained between about 1300～1500 ℃.

19. method as claimed in claim 17 is comprising the operating pressure in the reactor vessel is maintained about 5barg.

20. method as claimed in claim 17, the heat-transfer fluid that wherein circulates comprise fluid is circulated in the one or more passages between this first pressurized vessel and jacket structure.

21. method as claimed in claim 17, the heat-transfer fluid that wherein circulates comprise the fluid of circulation between this first pressurized vessel and second pressurized vessel.

22. method as claimed in claim 17 is wherein added liner with first pressurized vessel with coating material.

23. method as claimed in claim 17 comprising when reactor does not move, is being higher than 200 ℃ with the temperature maintenance of lining.

24. method as claimed in claim 17, comprising cooling off the first pressurized vessel wall part at the reactor run duration, and between the down-time period reactor heating lining.

25. method as claimed in claim 17, wherein carbonaceous material is a halogenide.

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