Patent Application
20110174744
This invention relates to a reactor and a method for supercritical water oxidation.
Supercritical water oxidation is a method for efficiently destructing organic pollutants in wastewater and sludge. The method is known to rapidly and efficiently transform the organic material comprising substantially carbon and hydrogen to carbon dioxide and water, often with an efficiency of above 99%.
The most efficient and inexpensive reactor layout is the tubular reactor. For wastewater streams containing solid organic material, the tubular reactor is the most practical solution since a given velocity is needed to transport the solid material through the reactor. Alternatively, a vertical bulk reactor is used, wherein the solid material is transported through the reactor by means of gravity. However, a drawback of using such a vertical reactor is that the solid material, which is heavier than supercritical water, is transported faster through the reactor with lower destruction efficiency as a result.
In U.S. Pat. No. 6,551,517 B1 a process for the conducting of chemical reactions in a fluid under pressure and at temperature in a supercritical fluid containing a solvent and at least one electrolyte such as a salt, in which reactive species are generated in situ by electrolysis, is disclosed. According to the invention, the fluid flows upwards in a reservoir reactor crossing through a first lower electrolysis zone with high salt solubility and a second upper zone in which the salts precipitate, then the fluid free of salt is evacuated at the upper part of the reservoir reactor and directed into a second tubular reactor to reach the desired stage of advancement of the conversion.
A drawback of the reactor system disclosed in B1 is that the oxidant is not fed to the reactor, but it is generated in situ by electrolysis. Hydrogen is also formed by the process, which has to be separated from the oxygen to avoid that the hydrogen and the oxygen immediately react with each other. It is believed to be expensive to produce oxidant in such a manner.
A further drawback is that due to the stream being directed from the bottom of the tank to the top thereof any solid material will sink to the bottom of the tank, and will thus not be transported together with the flow through the tank and through the second tubular reactor. If the solid material contains organic material, the destruction efficiency will thus be very low.
For some wastewater streams, a tubular reactor having short distances to the reactor walls may have its limitations. While treating wastepaper sludge to recover paper filler for the manufacturing of paper, some gypsum may form in the reactor immediately after the intake of the oxidant (due to formation of sulfuric acid that reacts with calcium carbonate in the filler). The gypsum may stick on the reactor walls and cause rather rapid local clogging of the reactor. Similar problems occur when treating municipal sludge if too high amounts of calcium and sulfur are present in the wastewater.
Another general problem with supercritical water oxidation comprises difficulties in treating wastewater streams containing dissolved salts. At conditions supercritical to water the salts become insoluble and the salts may be precipitated onto surfaces of a heat exchanger located upstream of the reactor causing the efficiency of the heat exchanger to drop. A solution to this problem is to mix a stream containing dissolved salts at conditions subcritical to water with a stream free from salts at conditions supercritical to water in the tubular reactor so that the mixed stream is at conditions supercritical to water. In this manner, a phase transition in a heat exchanger may be avoided and instead the precipitation of the salts occurs in the tubular reactor where the two streams are mixed. However, in some applications clogging of the tubular reactor occurs at this location due to that some salts are “sticky” when they are transformed from dissolved to solid state, and that the distances to the walls of the tubular reactor are short.
Another limitation when using tubular reactors for supercritical water oxidation is that for instance halogens are very corrosive at high but still subcritical temperatures for water and particularly at low pH values, in spite of the fact that corrosion resistant nickel-based alloys are used as construction material. If the halogen is comprised in an organic compound, no corrosion occurs until the organic compound is decomposed to carbon dioxide, water and halogen ion(s). To reduce the corrosion a pH neutralizing substance may be injected into an end portion of the reactor before the stream reaches subcritical temperatures for water. A common substance for pH adjustment is sodium hydroxide. However, a difficulty when feeding sodium hydroxide or similar alkaline is that these are hardly miscible with supercritical water. A melt is formed at supercritical temperatures for water, which is strongly corrosive to the material of construction.
The present invention provides a reactor and a method, respectively, that overcome, or at least reduce, the problems and limitations of the prior art reactors and methods as described above.
In accordance with a first aspect of the present invention there is provided a reactor for supercritical water oxidation, which comprises an essentially vertical reactor section, and an essentially non-vertical reactor section, wherein the vertical reactor section has a cross-sectional area which is substantially larger than the cross-sectional area of the non-vertical reactor section. Preferably, the vertical reactor section is a bulk reactor and the non-vertical reactor section is a tubular reactor. The vertical reactor section has an inlet in an upper portion of the vertical reactor section provided for receiving a flow containing organic material and water; the vertical reactor section is configured to oxidize organic material in the flow through supercritical water oxidation while the flow is flowed through the vertical reactor section from top to bottom; and the vertical reactor section has an outlet in a lower portion of the vertical reactor section provided for outputting the flow. The non-vertical reactor section is also provided for oxidizing organic material in the flow through supercritical water oxidation while the flow is flowed through the non-vertical reactor section, which may be arranged downstream or upstream of the vertical reactor section. Together the two reactor sections may efficiently oxidize essentially all organic material in the flow.
In a preferred embodiment the reactor is provided for the formation of solid and/or corrosive material within the vertical reactor section, preferably far from any reaction section walls, on which the solid may settle, and/or which walls may experience corrosion problems. Simultaneously, the reactor should prevent any formation of clogging and/or corrosive material in the non-vertical reactor section.
If the flow contains solid material, it may be transported through the vertical and non-vertical reactor sections in the same direction as the flow, and if the vertical reactor section is configured for precipitation of solid material from the flow, it may be transported through the vertical reactor section in the same direction as the flow, and if the non-vertical reactor section is located downstream of the vertical reactor section, the precipitated solid material may be transported also through the non-vertical reactor section in the same direction as the flow.
The reactor of the present invention severely reduces problems of clogging and corrosion.
Preferably, each of the two reactor sections is configured for oxidizing at least 5%, more preferably at least 10%, and most preferably at least 25%, of the organic material comprised in the flow. They may be configured to together oxidize virtually all organic material comprised in the flow if the reactor does not comprise further reactor sections.
In accordance with a second aspect of the present invention there is provided a method for supercritical water oxidation by using the reactor of the first aspect of the invention.
The present invention provides a reactor and a method for supercritical water oxidation, wherein problems with clogging and corrosion may be reduced, while very high destruction efficiency is maintained.
Other features and advantages of the invention will become more readily understood from the following detailed description taken in connection with the appended claims and attached drawings.
A reactor for supercritical water oxidation according to a first illustrated embodiment of the present invention is shown in
The vertical reactor section 11, which may be referred to as a bulk or reservoir reactor, is preferably substantially cylindrical having a diameter D, and the non-vertical reactor section 12, which may be referred to as a tubular reactor, is preferably substantially cylindrical having a diameter d, which is substantially smaller than the diameter D of the bulk reactor 11. In other words, the vertical bulk reactor section 11 has a cross-sectional area which is substantially larger than the cross-sectional area of the non-vertical tubular reactor section 12. The cross-sectional area of the bulk reactor section 11 may be at least two times, preferably at least three times, more preferably at least five times, and most preferably between about five and ten times, larger than the cross-sectional area of the tubular reactor section 12.
The bulk reactor section 11 has a first 14 and a second 15 inlet in an upper portion of the bulk reactor section 11, and an outlet 16 in a lower portion of the bulk reactor section 11.
The first inlet 14 is connected to receive a flow containing organic material and water such as wastewater or sludge as being schematically indicated by arrow 17. The bulk reactor section 11 is configured to oxidize part of the organic material in the flow through supercritical water oxidation while the flow is flowed through the bulk reactor section from top to bottom as being schematically indicated by arrow 19. The outlet 16 is provided for outputting the reacted flow at the bottom of the bulk reactor section 11 as being schematically indicated by arrow 20.
If the flow contains solid material, or if the bulk reactor section is configured for precipitation of solid material from the flow, this solid material is output at the outlet 16 of the bulk reactor section 11 together with the flow.
The tubular reactor section 12 is connected to the outlet 16 of the bulk reactor section 11 and is configured to very efficiently oxidize organic material, which was not oxidized by the bulk reactor section 11 through supercritical water oxidation.
The reactor may further comprise various sensors, such as flow and temperature sensors, as is generally known in the art. A computer is typically provided for the overall control of the reactor, and various control and regulation equipment is used for the control of the different streams. Pumps, valves, heaters and coolers are typically used for adjusting pressure and temperature.
By means of the reactor of the embodiment illustrated in
In a first exemplary version of the illustrated embodiment the flow also contains calcium and sulfur. Oxidant, particularly oxygen, is introduced through the inlet 15 as being schematically indicated by arrow 18 to oxidize the organic material in the flow. During the reaction, gypsum is rapidly formed, which is output through the outlet 16 together with the flow.
The flow may be sludge, particularly deinking sludge including a paper filler, or wastewater containing high amounts of calcium and sulfur.
Due to the large distances to the reactor walls in the bulk reactor section 11 the immediate formation of gypsum will not clog the reactor. Preferably, oxidant is added in an amount sufficient for further efficient oxidation in the tubular reactor section 12.
In a second exemplary version of the embodiment illustrated in
A flow that is at conditions subcritical to water and contains a dissolved salt that precipitate at conditions supercritical to water is entered into the bulk reactor section 11 through the inlet 15 as being schematically indicated by arrow 18. This flow may contain oxidizable material.
The supercritical and the subcritical flows are mixed in the bulk reactor section 11, the temperatures and flow rates of the supercritical and the subcritical flows are selected to obtain a mixed flow that is at conditions being supercritical to water, or becomes supercritical due to the heat of oxidation, to thereby precipitate the salt in the bulk reactor section 11, see U.S. Pat. No. 6,171,509, the contents of which being hereby incorporated by reference.
Preferably, the precipitated salt is output through the outlet 16 together with the mixed flow.
Due to the large distances to the reactor walls in the bulk reactor section 11 the precipitation of salts will not clog the reactor.
Thus, in the two examples above the reactor is provided for the formation of clogging material, i.e. gypsum and/or precipitated salt, within the bulk reactor section 11 only. Thus, no gypsum and/or precipitated salt are formed in the tubular reactor section 12.
The tubular reactor section 12 may be used in some cases only for minor oxidation.
With reference next to
Thus, a flow containing organic material and water is flowed first through the tubular reactor section 12, and then through the bulk reactor section 11, while at least part of the organic material in the flow is oxidized through supercritical water oxidation.
By means of the reactor of the embodiment illustrated in
In a first exemplary version of the illustrated embodiment the flow that is flowed through the reactor is at acidic conditions, and contains a substance corrosive at condition subcritical to water, i.e. sulfuric acid or hydrochloric acid.
A pH neutralizing agent or substance is introduced to the flow in the bulk reactor section 11 through the inlet 15 to neutralize the acid and reduce corrosion when water becomes subcritical, at some point downstream of the injection point, in the bulk reactor section 11. By introducing the pH neutralizing agent in the vertical bulk reactor, clogging due to the introduction of the pH neutralizing agent is minimized. Furthermore, if the pH neutralizing agent is caustic soda, which is known to form a melt that is very corrosive also at supercritical conditions to water, the introduction of it in the vertical bulk reactor will minimize the risk of said melt to adhere to the reactor walls and thus create serious corrosion. Obviously, no corrosive melt is formed in the tubular reactor section 12.
The corrosivity of the melt is disclosed in the article Review of the Corrosion of Nickel-Based Alloys and Stainless Steels in Strongly Oxidizing Pressurized High Temperature Solutions at Subcritical and Supercritical Temperatures, P. Kritzer et al., Corrosion—Vol. 56, No. 11, 2000, the contents of which being hereby incorporated by reference.
A second exemplary version of the embodiment illustrated in
In the embodiment of
With reference finally to
The first inlet 24 is connected to the tubular reactor section 12 to receive the flow as being schematically indicated by arrow 27; a further flow or substance is entered into the further bulk reactor section 21 through the second inlet 25 as being schematically indicated by arrow 28; and the material introduced into the bulk reactor section 21 is flowed from top to bottom as being indicated by arrow 29 while the material is chemically reacted. Any organic material contained in the bulk reactor section 21 is oxidized through supercritical water oxidation. Finally, the reacted material is output through the outlet 26 as being schematically indicated by arrow 29.
In an exemplary version of the embodiment illustrated in
It shall be appreciated that any bulk reactor section of the present invention may be configured and used in accordance with more than one of the above described exemplary versions simultaneously.
Thus, a flow that contains calcium and sulfur, is at conditions supercritical to water, and is essentially free from salts that precipitate at conditions supercritical to water may be entered through the inlet 14 of the bulk reactor section 11 of
Alternatively, or additionally, a flow that is at conditions supercritical to water, is essentially free from salts that is dissolved in liquid water and that precipitate at conditions supercritical to water, is at acid conditions, and contains a corrosive substance may be entered through the inlet 14 of the bulk reactor section 11 of
It shall further be appreciated that a reactor of the present invention may comprise two or more tubular reactor sections, and one or more essentially bulk reactor sections, wherein each of the tubular reactor sections has a cross-sectional area which is substantially smaller than the cross-sectional area of each of the bulk reactor sections.
It shall still further be appreciated that the present invention may be implemented as a multistage reaction system as being disclosed in e.g. U.S. Pat. No. 5,770,174, the contents of which being hereby incorporated by reference. Here, each of the reactor sections is provided for oxidizing part of the organic material comprised in the flow. Each reactor stage is designed to oxidize as much as possible of the organic material without exceeding a pre-determined maximum temperature which, for instance, may be dictated by material of construction limitations.
Investigations were conducted to verify the result of the present invention.
Waste paper sludge was fed through a supercritical water oxidation plant having a conventional tubular reactor in a number of tests. Each of the tests had to be interrupted after less than 17 hours of operation due to clogging of the reactor. A plug of calcium sulphate, gypsum, and of a few tens centimeters in length was formed immediately downstream of the oxygen inlet. Despite the low amount of gypsum relative the amount of other inorganic material in the process stream, the gypsum creates severe problems since it precipitates so rapidly directly when the oxygen has been introduced, and since it has a strong adhesive capacity.
Subsequently, waste paper sludge was fed through a supercritical water oxidation plant having a reactor as the one illustrated in
| Number | Date | Country | Kind |
|---|---|---|---|
| 0402783.5 | Nov 2004 | SE | national |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 11666638 | Oct 2007 | US |
| Child | 12973334 | US |
