text:
|Publication number
|Publication type
|Application number
|Publication date
|Sep 6, 1988
|Filing date
|Sep 25, 1986
|Priority date
|Sep 25, 1986
|Fee status
|Also published as
|Publication number
|Russell L. McGalliard
|Original Assignee
|Amoco Corporation
|Export Citation
|BiBTeX, EndNote, RefMan
|Patent Citations (5), Referenced by (7), Classifications (10), Legal Events (4)
|External Links: USPTO, USPTO Assignment, Espacenet
The invention relates to the removal of sulfur and sulfur compounds from gaseous streams containing such compounds. In one aspect, the invention relates to the removal of sulfur compounds including H2 S (hydrogen sulfide) and SO2 (sulfur dioxide) from Claus plant tail gas. In another aspect, the invention relates to the use of solid high surface area contact materials (absorbents), for example, ZnO-based (zinc oxide-based) absorbents, for absorbing sulfur compounds such as SO2 and H2 S. In a further aspect, the invention relates to regenerating sulfided ZnO-based absorbents (zinc sulfide, ZnS) under conditions for reducing the rate of regeneration effluent, and increasing the concentration of sulfur and sulfur compounds, returned to the Claus plant. In another aspect, the invention relates to absorbing sulfur compounds from a Claus plant tail gas stream using a metal oxide absorbent and regenerating the resulting sulfided absorbent in a way that reduces the size of absorber required.
A developing area of sulfur recovery technology is that of tail gas cleanup, that is, of removing trace quantities of sulfur compounds from gaseous effluent streams (tail gas) of Claus process sulfur recovery plants. Tail gas may contain substantial amounts of sulfur compounds. Tail gas from Claus or extended Claus plants (having at least one Claus catalytic reaction zon operated under conditions, including temperature, effective for depositing a preponderance of formed sulfur on catalyst therein) typically can contain about 0.5-10% of the sulfur present in feed to the plant as elemental sulfur, H2 S, SO2, COS (carbonyl sulfide), CS2 (carbon disulfide), and the like. Tail gas cleanup processes remove at least part of such residual sulfur compounds from Claus tail gas.
In U.S. Pat. No. 4,533,529, Claus tail gas is contacted with ZnO (zinc oxide) in an absorber reducing average overall emission levels from the absorber to less than 250 ppm sulfur species. When ZnS is being regenerated to its active ZnO form, producing SO2, the resulting regeneration effluent stream comprising SO2 can be returned to the Claus plant for removal of SO2 by conversion to elemental sulfur.
Reducing the rate of return of such a regeneration effluent stream to the Claus plant can result in highly significant cost savings in plant construction and retrofits as well as in operation and maintenance. This is because providing the regeneration effluent stream to the Claus Plant in addition to the Claus Plant acid gas feed increases the total feed rate of gaseous streams to the Claus Plant. The result is an increase in size of the Claus Plant downstream of the site at which the regeneration effluent stream is returned. Hence, reducing the rate of return of such a regeneration effluent stream to the Claus plant can reduce the size of Claus plant required.
There is provided a process which can reduce the rate of regeneration effluent, and increase the concentration of sulfur compounds, returned to a Claus plant and can achieve the significant economic and technical benefits resulting therefrom.
According to an alternative aspect of the invention, there is provided a process which can reduce the size of absorber required for reducing sulfur compound content of Claus plant effluent to be discharged to the atmosphere to an environmentally desirable level.
In according with further aspects of the invention, there is provided a process in which the advantages of reducing the rate of regeneration effluent return to the Claus plant and of reducing the size of absorbers required for absorption can both be achieved, thus providing a greater flexibility in design and operation of such plants.
The present invention comprises an improved process and system for the recovery of sulfur and sulfur compounds from a gaseous stream. The sulfur compounds are removed from the gaseous stream in the presence of metal oxide absorbent (ZnO-based absorbent) in an absorber to produce a laden (sulfided) absorbent (ZnS) and a gaseous stream reduced in sulfur compound content. The laden absorbent ZnS is then regenerated in a regenerator by withdrawing a portion of the gaseous stream upstream of the absorber and blending the withdrawn portion with an oxygen-containing stream which is passed in contact with the absorbent, producing a regenerated absorbent (ZnO) and a regenerator effluent stream. The regenerator effluent is returned to the Claus plant. Use of absorber feed as a source of diluent for oxygen during regeneration reduces the absorption rate in the absorber, allowing regeneration to be conducted at a lower rate, reducing the recycle rate of regenerator effluent to the Claus plant, and increases the concentration of sulfur and sulfur compounds and the regenerator effluent returned to the Claus plant. Alternatively, the reduction in absorption rate can be advantageously translated into a reduction in the size of absorber required. These results can be achieved in accordance with the invention by not passing the portion of Claus plant gas-in-process used for regeneration diluent through the absorbers.
In one aspect, the invented process comprises removing sulfur compounds from a Claus plant tail gas comprising H2 S, SO2, organic sulfides such as carbonyl sulfide (COS), carbon disulfide (CS2) and the like, and elemental sulfur. The tail gas is provided to an absorber containing a metal oxide absorbent (ZnO-based absorbent) effective for removal of at least H2 S from the stream. H2 S in the stream is absorbed by the metal oxide absorbent (ZnO) producing sulfided absorbent (ZnS) and absorber effluent. The sulfided absorbent ZnS is then regenerated in a regenerator by withdrawing a portion of absorber feed upstream from the absorber and blending the withdrawn portion with an oxygen-containing stream, and then passing the resulting dilute oxygen-containing stream in contact with the sulfided absorbent ZnS producing a regenerated absorbent ZnO and regeneration effluent. The regenerator effluent is provided back to the Claus plant where sulfur compounds therein are converted to elemental sulfur and removed.
In a further aspect, the process comprises removing sulfur compounds from a Claus plant tail gas stream having at least one Claus low temperature catalytic absorption zone operated under conditions, including temperature, such that a preponderance of elemental sulfur formed is deposited on the Claus conversion catalyst.
By withdrawing a portion of absorber feed upstream of the absorber containing metal oxide absorbent, and using that portion as a diluent for oxygen during regeneration, the rate of regenerator effluent recycled back to the Claus plant can be significantly reduced in comparison to a process which utilizes absorber effluent as a diluent stream. See, for example, U.S. Pat. No. 4,533,529 (1985). Withdrawing a portion of the absorber feed upstream from the absorbent reduces the rate of sulfur compound containing gaseous feed introduced into contact with the absorbent in the absorber. As there is a smaller quantity of sulfur compounds to be absorbed by the absorbent per unit time, the absorber loading rate is decreased. Then, the rate at which the absorbent is regenerated in the regenerator can correspondingly be decreased, thereby decreasing the rate at which regeneration effluent is recycled to the Claus plant for further sulfur recovery. Reducing the rate at which recycle is provided to the Claus plant results in a reduction in the total gaseous feed rate to the Claus plant. Hence, the rate at which gaseous effluent is produced from the Claus plant is reduced, and therefore the rate at which such effluent is processed in the absorber is likewise reduced. The end result is a significant reduction in the sizing of equipment required for a Claus plant with metal oxide absorbers for tail gas cleanup with a corresponding reduction in capital and operating costs.
Alternatively, the benefits of not passing the portion of Claus plant tail gas required for regeneration diluent through the absorber can be utilized in achieving a reduction in the size of absorber required. Further, combinations of these advantages will be apparent to those skilled in the art from the present disclosure.
The invention accordingly comprises the processes and systems, together with their steps, parts, and interrelationships which are exemplified in the present disclosure, and the scope of which will be indicated in the appended claims.
The FIGURE shows schematically an embodiment of the invention.
The invention comprises introducing a sulfur and sulfur compound containing gaseous stream into an absorber zone containing ZnO effective for removing at least H2 S from the gaseous stream under conditions, including temperature and composition, for such removal, producing sulfided absorbent ZnS and absorber effluent reduced in sulfur compound content. ZnS is regenerated in a regenerator by withdrawing a portion of absorber feedstream upstream of the absorber and blending the withdrawn portion with an oxygen-containing stream and then passing the resulting oxygen-containing stream in contact with ZnS regenerating the absorbent to ZnO and producing regenerator effluent. Regenerator effluent is recycled back to the Claus plant for further sulfur recovery.
The portion of absorber feed withdrawn upstream of the absorber for use as a regeneration diluent can be any suitable gas-in-process in the the Claus plant or can be the Claus plant tail gas. Thus, the diluent stream can be withdrawn downstream of a sulfur condenser following a first or subsequent Claus catalytic reactor, or preferably can be the Claus plant tail gas feed itself to the absorbers.
In the Claus plant, sulfur is recovered from an H2 S-containing stream by introducing the stream into a thermal reaction zone (Claus furnace) and at least one Claus catalytic reaction zone. The Claus thermal reaction zone can be, for example, a Claus muffle furnace, a fire tube (tunnel) furnace, or the like. Generally, the Claus thermal reaction zone functions for converting a portion of H2 S, preferably about 1/3, to SO2 for thermal or catalytic Claus reaction with H2 S to form elemental sulfur.
In the Claus furnace, the H2 S-containing gas and oxidant can be reacted at a temperature generally in the range of about 1800�-2600� F. The effluent from the Claus thermal reaction zone can be cooled, for example, in a waste heat boiler, and optionally passed through a sulfur condenser to condense and remove liquid sulfur.
The gaseous effluent can then be fed into a Claus catalytic reaction zone operated above the sulfur dewpoint having an inlet temperature in the range, for example, of about 350�-650� F. In the Claus catalytic high temperature catalytic reactor, sulfur is formed by the Claus reaction (shown below) in the presence of an effective Claus reaction-promoting catalyst such as alumina or bauxite:
Elemental sulfur vapor can be continuously removed from the reactor and provided to a sulfur condenser where it is condensed and removed as a liquid. Gaseous effluent from the sulfur condenser can be reheated, if desired, and passed to further high temperature Claus reactors and associated sulfur condensers as is known in the art. The effluent gas from the final sulfur condenser is then the Claus plant tail gas.
Preferably, the Claus plant tail gas is from a Claus plant which includes at least one Claus catalytic reactor operated under conditions, including temperature, effective for depositing a preponderance of the formed sulfur on Claus catalyst therein. Such a Claus low temperature adsorption zone can be broadly operated in the range of from about 160� to about 330� F., preferably in the range of from about 260�-320� F.
The operation of such Claus plants having Claus high temperature reactors and Claus low temperature adsorption reactors is well known in the art and need not be further described here.
The tail gas from such Claus plants comprises H2 S, SO2, organic sulfides, and reducing species such as H2 and CO. Tail gas from plants having only Claus high temperature reactors can contain H2 S in the range of about 0.4 to about 4 mol %, SO2 in the range of about 0.2 to about 2 mol %, water in the range of about 20 to about 50 mol % (typically 30-40 mol %), as well as organic sulfides such as COS and CS2, and elemental sulfur. Where the tail gas is from a plant having one or more Claus low temperature adsorption reactors, the tail gas may have equivalent of about 0.4 mol %, preferably about 0.2 mol %, or less single sulfur species.
Use of at least one Claus low-temperature adsorption reactor is preferable in part because such reactors remove significant amounts of organic sulfides, such as COS, CS2, and the like from the gas in process. These organic sulfides are not removed by sulfur recovery processes such as the IFP process described in DeZael, et al., U.S. Pat. 4,044,114 (1977) which forms elemental sulfur in the presence of polyethylene glycol and sodium benzoate.
For the same reason, it is also preferred to operate at least one Claus high temperature reactor so that effluent has a temperature in the range from about 550� to 700� F., preferably from about 600� to 650� F. to diminish the amount of organic sulfides in the effluent.
Both H2 S and SO2, as well as organic sulfides, can be concurrently removed in the absorber in the presence of reducing species for reducing the SO2 and other sulfur species to H2 S. Alternatively, sulfur species other than H2 S can be converted to H2 S in a hydrogenation zone prior to introduction into the absorber. In either case, it is preferred to operate the Claus plant so that about a 2:1 ratio of H2 S:SO2 is maintained in the Claus plant tail gas to maximize sulfur recovery in the Claus plant and to minimize the amount of sulfur remaining in the Claus plant tail gas to be removed by the ZnO absorbers. By reducing the organic sulfide and other sulfur content in the feed to the absorbers, the volume of regeneration effluent returned to the Claus plant can be diminished. An effect of operating at about a 2:1 ratio is that significant quantities of both H2 S and SO2 are present in the Claus plant tail gas.
The reducing species, for example, H2, and/or CO required for conversion of sulfur compounds in the tail gas to H2 S can be obtained from any convenient source including that present in the tail gas as H2, or available from a donor such as CO, which can react with water to yield H2. H2 is preferred, whether contained in the tail gas or internally generated or provided from an outside source.
The Claus plant tail gas can contain sufficient reducing species where the Claus plant is appropriately operated. For most Claus plants, by operating the Claus furnace so that slightly less air is utilized than that required for reaction (1)
and by insuring that the tail gas leaving the final sulfur condenser of the Claus plant has a low level of residual elemental sulfur, the Claus plant tail gas will contain sufficient reducing species. By further reducing the amount of oxidant introduced into the Claus furnace or by other methods which will be apparent to persons skilled in the art, the amount of reducing species can be further increased if desired.
The Claus plant tail gas having sufficient reducing species to reduce all sulfur compounds therein to H2 S can be heated, for example, directly by means of direct fired heaters, or indirectly by heat exchange, for example, with other process streams such as absorber effluent, to produce a heated Claus plant tail gas effluent stream having a temperature effective for removal of both H2 S and SO2 in the presence of a solid particulate preferably high surface area (for example, pellets, extrudates, and the like) ZnO absorbent effective for such removal. This simultaneous removal of both H2 S and SO2 is considered to proceed by hydrogenation of sulfur compounds present in the tail gas to H2 S in the presence of ZnO, ZnO in this respect acting as a catalyst, followed by absorption of the thus-formed H2 S by the ZnO by sulfiding the ZnO to ZnS, the ZnO acting as an absorbent. Preferably, the Claus plant tail gas can be heated to above about 1000� F. By operating at these absorber temperatures, a hydrogenation reactor is not required before removal of H2 S and other sulfur compounds in the absorber. Conversely, temperatures below about 1000� F. can be used during absorption with the addition of a separate and distinct hydrogenation reactor or zone prior to the absorbers. When operating at temperatures above about 1000� F., H2 S emissions can set a practical upper limit on the absorption temperature which will be used. Currently for these reasons it may be appropriate that the upper limit during absorption be about 1200� F. Higher temperatures can also be used. Absorber operation above about 1000� F. is preferred because such higher temperatures favor higher absorption capacity and the hydrogenation reactor can be eliminated. Also, since absorption and regeneration will then be conducted at approximately the same inlet temperature (1000�-1200� F.), temperature stress on equipment can be reduced. As a result, there will be no significant heating and cooling period. Hence, the time available for regeneration and absorption will be increased and the volume of regeneration effluent returned to the Claus plant can be decreased.
Where the Claus plant tail gas is introduced into a hydrogenation zone prior to the ZnO absorbers, the principal reaction will be the conversion of SO2 to H2 S as shown by Reaction (6) below; other sulfur compounds including elemental sulfur, COS, CS2, and the like will also be reduced to H2 S. Hydrogenation can be carried out at a temperature of from about 450� to about 1200� F. or even higher, preferably from about 580� F. to about 800� F., depending on the conditions and the source of H2 chosen. Hydrogenation by contacting with a bed, either supported or fluidized, of effective hydrogenation catalyst is preferred. Useful catalysts are those containing metals of Groups VB, VIB, VIII and the Rare Earth series of the "Periodic Table of the Elements" in Perry and Chilton, Chemical Engineers Handbook, 5th Ed. The hydrogenation catalyst may be supported or unsupported. Catalysts supported on a refractory inorganic oxide, such as on a silica, alumina or silica-alumina base are preferred. The preferred catalysts are those containing one or more of the metals, cobalt, molybdenum, iron, chromium, vanadium, thorium, nickel, tungsten (W) and uranium (U) added as an oxide or sulfide of the metal, although the sulfide form appears to be the active form. Particularly preferred are cobalt-molybdenum hydrogenation catalysts such as are commercially available for use in the refining industry for desulfurization processes in the refining of oil.
After hydrogenation, the resulting stream now containing substantially all sulfur compounds in the form of H2 S can then be contacted in an absorber zone with a suitable ZnO absorbent (either fixed or fluidized bed) to absorb H2 S and to produce a laden (sulfided) absorbent at temperatures in the range of about 600� F. to about 1000� F. Alternatively, where absorption is conducted at a temperature above about 1000� F., for example, in the range of about 1000� F. to about 1200� F., the absorption of H2 S can be accomplished in an absorber simultaneously with removal of the other sulfur compounds without prior hydrogenation. In either event, while a first absorption zone is functioning as an absorber, a second absorption zone can be functioning as a regenerator.
As used herein, and in the claims, the terms "metal oxide absorbent", "ZnO", "ZnO absorbent", and the like shall mean an absorbent effective for removal of both H2 S and SO2 in the presence of reducing species. A major portion of the active absorbent, for example, fifty percent or more, is in the form of ZnO which is the active form. The absorbent can also contain binders, strengtheners, and support materials, for example, alumina (Al2 O3), calcium oxide (CaO) and the like. Zinc sulfide and zinc sulfate can be used as starting materials and treated with heat and/or oxygen to produce an active ZnO absorbent. Other suitable starting materials can also be used. The ZnO absorbent is effective for absorbing H2 S by undergoing sulfidization to produce a laden (sulfided) absorbent; simultaneously, if desired, hydrogenation of other sulfur compounds to H2 S followed by such absorption can occur. Preferably, the ZnO absorbent is capable of a high level of removal of sulfur compounds and is relatively insensitive to water.
Particularly preferred are ZnO absorbents which are thermally stable, regenerable, and capable of absorbing substantial amounts of sulfur compounds. An acceptable absorbent is United Catalysts, Inc., G72D Sulfur Removal Catalyst, available from United Catalysts, Inc., Louisville, Ky., having the following chemical composition and physical properties:
______________________________________CHEMICAL COMPOSITIONwt % Trace Metal Impurities wt %______________________________________ZnO 90.0 � 5% Pb <0.15Carbon <0.20 Sn <0.005Sulfur <0.15 As <0.005Chlorides <0.02 Hg <0.005Al2 O3 3-7 Fe <0.1CaO 0.5-3.0 Cd <0.005______________________________________
______________________________________PHYSICAL PROPERTIES______________________________________Form PelletsSize 3/16 in.Bulk Density 65 � 5 lbs/ft3Surface Area 35 m2/g minimumPore Volume 0.25-0.35 cc/gCrush Strength 15 lbs minimum average______________________________________
Representative chemical reactions considered to occur during absorption, regeneration and purging are shown below:
During absorption:
H2 S+ZnO→ZnS+H2 O (3)
COS+ZnO→ZnS+CO2 (4)
CS2 +2ZnO→2ZnS+CO2 (5)
H2 S+Sulfated Absorbent→SO2 +ZnO Absorbent (7)
During absorption, H2 S, COS and CS2 in the stream can react with ZnO to form ZnS as shown in Eqs. (3) to (5). SO2 can react directly with H2 to form H2 S as shown by Eq. (6), and the resulting H2 S can then react with ZnO. COS and CS2 may also be hydrogenated to H2 S before absorption by ZnO. When elements in the absorbent such as zinc, calcium, aluminum, or other elements become sulfated during regeneration, SO2 may be produced during absorption as indicated by Eq. (7) due to the presence of effective reducing species in the absorber feed. Sulfation is reversed by purging the regenerated absorbent with effective reducing species before returning regenerated ZnO to absorption and returning the produced SO2 to the Claus plant for sulfur formation and removal.
During Regeneration:
ZnS+3/2O2 →ZnO+SO2 (8)
Absorbent+SO2 +O2 →Sulfated Absorbent (9)
Regeneration of sulfided absorbent is effected by oxidizing ZnS to ZnO as shown by Eq. (8). Absorbent sulfation can also occur, as shown by Eq. (9) during regeneration in the presence of O2 and SO2. Temperature rise during regeneration can suffice if unchecked to destroy both the physical integrity and the chemical activity of the absorbent as well as to exceed metallurgical limits of preferred materials of construction. Consequently, temperature rise during regeneration is preferably controlled to less than about 1500� F.
During Purging:
Sulfated Absorbent+H2 →Absorbent+SO2 +H2 O (10)
Sulfated Absorbent+CO→Absorbent+SO2 +CO2 (11)
Sulfated Absorbent+H2 S→Absorbent+SO2 +H2 O (12)
Reduction of the sulfated absorbent will occur at a temperatures above about 1000� F. in the presence of H2, CO or other reducing species such as H2 S. Reduction of the sulfated absorbent does not occur at lower temperatures such as 900� F. or lower or in the absence of such effective reducing species.
Methane, although a reducing gas, may not be effective in reasonable periods of time under process conditions for purging. Further, purging with an inert gas will not prevent the SO2 emissions increase upon returning to absorption. Rather, upon switching to absorption, the sulfated ZnO absorbent will be contacted with a stream containing the effective reducing species (H2, CO, and H2 S) and SO2 emissions will occur. Accordingly, for the purging, it is essential that effective reducing species be present and that the temperature be greater than about 1000� F.
The absorber zone containing ZnO can comprise at least a first absorption zone (functioning as an absorber) and a second absorption zone (functioning as regenerator) and the process can comprise contacting H2 S with absorbent in the absorber to remove it and other sulfur species producing a laden absorbent and absorber effluent lean in sulfur species. Absorption can be continued for a period of time (absorption), preferably less than that required for H2 S breakthrough from the absorber. For practical purposes, H2 S breakthrough can be defined as occurring when the H2 S concentration in the absorber effluent stream reaches a preset low value, such as for example, 50 ppm H2 S. Concurrently, with absorption in the absorber, laden absorbent in the regenerator can be regenerated by introducing a regeneration stream comprising dilute O2 thereinto at a temperature effective for converting laden sulfided absorbent to active absorbent. In accordance with the invention, a portion of absorber feed upstream of the absorber is utilized for diluting the O2 to produce the dilute O2 containing regeneration stream. Regeneration effluent comprising SO2 is returned from the regenerator to the Claus plant, for example, to the thermal reaction zone or to a downstream Claus catalytic reaction zone. Thereafter, the absorber and the regenerator can be interchanged, with the second absorption zone now functioning as absorber and the first absorption zone now functioning as a regenerator, and the process can be repeated and continued. Prior to interchanging the absorber and the regenerator, freshly regenerated absorbent in the regenerator is purged with an effective reducing gas. For example, purging can be conducted by discontinuing the introduction of O2 into the portion of absorber feed utilized for diluent during regeneration, and continuing flowing of the thus withdrawn portion of absorber feed for a period of time effective for reducing to a desired level an otherwise observed temporary increase in SO2 occurring where a freshly regenerated ZnO-based absorbent is returned to absorption without such purge.
During regeneration of ZnS to ZnO, a temperature rise of about 145� F. occurs for each mol percent of oxygen consumed in converting ZnS back to ZnO. To avoid exceeding about about 1500� F. and to maintain absorbent physical and chemical integrity during regeneration, a maximum of about 3.5 mol % oxygen can be used during regeneration when the regeneration stream is introduced at about 1000� F., and a maximum of about 2.75 mol % O2 when the regeneration stream is introduced at about 1100� F. Thus, preferably oxygen is introduced during regeneration at a concentration of about 0.4 or less to about 3.5 mol %, more preferably at about 1 to about 2.75 mol %. Due to the exothermic nature of the regeneration reaction, suitable methods for diluting the oxygen can be used. Higher temperatures of regeneration up to about 2100� F. can also be used and the amount of O2 introduced increased accordingly.
The flow rate during regeneration is preferably a rate sufficient to complete regeneration and purging as described herein of a ZnO absorber while absorption is conducted in another ZnO absorber. In this way, only two absorption zones will be required. Some time can also be allowed for the contingency of process upsets (slack time). Preferably, the flow rate during regeneration is such that the period during which regeneration is occurring is substantially equal to the period during which absorption is occurring less the period required for purging as herein set forth and such slack time.
As indicated, regeneration effluent comprising SO2 is returned from the regenerator to the Claus plant for conversion of the SO2 to elemental sulfur which is removed from the gas in process. Dilution of the O2 using absorber feed reduces the rate of regeneration effluent being returned to the Claus plant and increases the concentration of sulfur and sulfur compounds returned to the Claus plant. This has the desired result of decreasing the size of the Claus plant and equipment downstream of the locus where the regeneration effluent is reintroduced resulting in significant cost decreases as compared with other sources of gas diluent. Further, the increased concentration of sulfur and sulfur compounds in the regenerator effluent return to the Claus plant facilitates maintenance of stable flame temperatures and conditions in the Claus furnace. Alternatively, the size of absorbers required for treatment of the Claus plant tail gas can be reduced.
Absorber feed can be used for diluent and the rate of regeneration effluent returned to the Claus plant can be still further reduced where the Claus plant comprises at least one Claus low-temperature absorption reactor.
By use of such a low-temperature Claus adsorption reactor, the absorption rate for a ZnO absorber is decreased in comparison with the rate where such a Claus low-temperature adsorption zone is not used, allowing O2 to be introduced to the regenerator at a still lower rate, further reducing the rate at which regeneration occurs, and further reducing the rate at which regeneration effluent is returned to the Claus plant.
Regeneration can be continued until substantially all of the sulfided absorbent is regenerated, for example, until ZnS is substantially reconverted to ZnO. Completion of regeneration can be conveniently determined by monitoring O2 or SO2 content or temperature of the regenerator effluent stream. Preferably, an O2 analyzer is employed downstream of the regenerator to determine the presence of O2 in the regenerator effluent, which is an indication of completion of regeneration.
As will be appreciated by those skilled in the art from the foregoing discussion, materials of construction for the valves, vessels, and piping for the process according to the invention can require special attention. The material preferably has the capability of withstanding high temperatures, for example, in the range of about 800� F. to about 1500� F. or higher while being repeatedly exposed to reducing and oxidizing atmospheres in the presence of sulfur compounds.
Following regeneration, prior to returning the regenerated absorbent for use during the absorption cycle, the regenerated absorbent is treated (purged) by passing a reducing stream in contact with the regenerated, albeit sulfated absorbent, for a period of time effective for reducing a temporary increase in SO2 emissions otherwise occurring when freshly regenerated ZnO absorbent is returned to absorption without such purging with a reducing gas. Preferably, the time is effective for reducing SO2 emissions to below about 250 ppm at all times. Most preferably, the time is effective for substantially eliminating the increase in SO2 emissions, that is, for reducing the increase in SO2 emissions by 90% or more from the level occurring where such a reducing gas purge is not used prior to returning to absorption.
The effective purge time can be readily determined by one skilled in the art by monitoring SO2 emissions from an absorber following returning a freshly regenerated reactor to absorption function and increasing the purge time prior to returning to absorption until the SO2 emissions are reduced to a desired level upon returning to absorption.
The purge stream can comprise a portion of absorber effluent or any other suitable reducing gas stream. In accordance with the invention, the purge is preferably effected by using the same portion of absorber feed used for diluent during regeneration, by discontinuing the flow of O2 to the regenerator during the purge period.
The invention will be further understood and appreciated from the following EXAMPLE.
Sizing of absorbers is calculated using data from a demonstration plant. The effects of using absorber feed or absorber effluent for regeneration diluent is evaluated for two cases. In Case I, the feed to the ZnO absorber is effluent from a Claus plant having three catalytic reactors operated above the sulfur dewpoint. In Case II, the feed to the ZnO absorber is effluent from a Claus plant having two catalytic reactors operated above the sulfur dewpoint and having at least one catalytic reactor operated under conditions, including temperature, effective for depositing a preponderance of sulfur form on the catalyst therein. The results of using absorber feed or absorber effluent on the relative size of absorbers for the two cases are shown in the following Table.
TABLE______________________________________Regeneration Diluent Relative Size of Absorbers______________________________________Case I Absorber Feed 1.0Case I Absorber Effluent 1.7Case II Absorber Feed 1.0Case II Absorber Effluent 1.3______________________________________
The results indicate that the use of absorber feed for regeneration diluent reduces the size of absorber required. Comparison of Case I and Case II indicates that the use of absorber feed has a greater relative effect in reducing the size of absorbers required when the sulfur content of the absorber feed is greater, as in Case I than when the sulfur content of the absorber feed is greater (Case I) than when content is lesser (Case II).
Referring now to the FIGURE, an exemplary embodiment of the invented process is represented in which the gaseous effluent stream from a 3-reactor Claus plant having two reactors (R2, R3) periodically operated under conditions, including temperature, effective for depositing a preponderance of formed elemental sulfur on catalyst therein, is provided to an absorber containing metal oxide absorbent in which H2 S, and preferably also SO2, are absorbed therefrom at temperatures above about 1000� F.
An acid gas stream containing H2 S and an O2 containing stream are fed into a furnace 3 by lines 1 and 2, respectively, and combusted to produce effluent gas, comprising elemental sulfur, uncombusted H2 S, SO2, and water. Effluent from the furnace 3 is cooled in a waste heat boiler 4. A resulting gas stream, for example, at a temperature of about 550� F., is passed by line 5 to first sulfur condenser 6 which condenses vaporized elemental sulfur from the stream. The gas stream leaves the first sulfur condenser 6 by line 7 at a temperature, for example, of about 400� F. Hot gas from the waste heat boiler 4 is also introduced by line 9 having valve 9V into line 7 leaving the first condenser 6 at a rate so that the gas stream in line 11 is, for example, about 450� F.-600� F. The gas stream 11 is passed to a first catalytic reactor 13 where further conversion of H2 S and SO2 into elemental sulfur occurs above the sulfur dewpoint in the presence of an effective Claus reaction promoting catalyst, and the resulting elemental sulfur is continuously removed in the vapor phase.
The gaseous effluent stream from the first catalytic reactor 13 is provided to a second sulfur condenser 101 by line 14 and condensed elemental sulfur is removed as shown. The gas stream leaving the second condenser by line 103 flows to a second catalytic reactor 106 on adsorption by line 105, having an associated valve as shown. During adsorption, the second catalytic reactor 106 inlet temperature is preferably maintained at a temperature in the range of about 250� F. to about 280� F. The gaseous effluent stream from the second catalytic reactor 106 leaves by line 107, having an associated valve as shown and is provided by line 110 to a condenser/cooler 111 functioning during adsorption as a cooler. The gas stream then leaves the condenser/cooler 111 by line 113 and is provided to a third catalytic reactor 117 by line 113, line 115, having an associated valve as shown, and line 116. The third catalytic reactor 117 is also operated under conditions, including temperature, such that a preponderance of formed elemental sulfur is deposited on the catalyst therein.
Periodically, catalyst having sulfur deposited thereon in the catalytic reactor 106 can be regenerated by passing a portion of the hot gaseous effluent stream from the first catalytic reactor 13 by line 136, having an associated valve therein, and line 103 to second catalytic reactor 106. During regeneration, elemental sulfur is vaporized from the catalyst, and the vaporized elemental sulfur can be condensed from the stream in the third condenser/cooler 111, and elemental sulfur can be removed as shown.
In the illustrated embodiment, the gaseous stream in line 103 is provided to reactor R2. By closing the valves in lines 105, 107, 115, and 119 and by opening the valves in lines 130, 131, 132, and 133, reactors R2 and R3 can be interchanged so that the gas stream in line 103 first flows to reactor R3. This will be done when the reactor R3, originally in the downstream position, which takes the longest to become laden with sulfur, is in need of regeneration. Thereafter, regeneration and adsorption can occur in R3 with reactor R2 in the downstream position until reactor R2 is again laden and switching will again occur. The operation of such plants is known to those skilled in the art and need not be further described here.
The gaseous effluent stream in line 120 from the Claus plant (Claus plant tail gas) in accordance with the invention is divided into two portions. One portion, is passed through line 140 around the ZnO absorbers. The second portion is passed to a ZnO absorber, for example, absorber 46 by line 120, blower 40, line 41, and heater 42. Heater 42 functions for heating the stream to a temperature above about 1000� F., and the resulting heated stream is introduced by line 44 having an associated valve into the first absorber 46 (shown on absorption). Second absorber 60 is shown on regeneration. (Following regeneration and purging as herein described, the first and second absorbers can be interchanged by closing the valves in lines 44, 49, 51, and 63 (shown open), and by opening valves in lines 71, 72, 73, and 74 (shown closed). In this mode, second absorber 60 will be on absorption and first absorber 46 will be on regeneration and purging.)
The first absorber zone 46 containing ZnO removes sulfur compounds from the portion of Claus plant tail gas introduced and produces absorber effluent containing less than about 50 ppm H2 S. The absorber effluent can be conducted by lines 49 and 50 and by heat recuperator 71 for discharge.
In accordance with the invention, the portion of Claus plant tail gas stream withdrawn by line 140 in valve l40V is employed via blower 142 for dilution of atmospheric air or other oxygen-containing gas provided via compressor 154 and line 55 having an associated valve therein, to produce a dilute oxygen containing regeneration stream in line 52.
The regeneration stream in line 52 is heated in heater 53 to regeneration temperatures and can be conducted by lines 56 and 51, having an associated valve therein, to second absorber 60 (shown on regeneration). The heated regeneration stream is thus passed in contact with sulfided absorbent in second absorber 60 to produce regeneration effluent containing SO2. The regeneration effluent is conducted by line 63 having an associated valve therein and by line 65 back to the Claus plant, for example to the furnace 3. The regeneration effluent can also be provided to a downstream catalytic reaction zone. Following regeneration, purging can be effected in accordance with the invention by discontinuing oxygen to the second absorber 60, for example, by closing the valve in line 54, and continuing to pass the portion of Claus plant tail gas through the absorber on regeneration for a period of time sufficient to reduce or eliminate an otherwise observed increase in SO2 emissions which occurs when freshly regenerated absorbent is contacted with a reducing gas stream, such as, for example, absorber feed. During this purge period, the effluent from the freshly regenerated absorber can continue to be provided to the Claus plant as during regeneration.
Absorption is continued in the first absorber 46 and regeneration is continued in the second absorber 60 until prior to or just before H2 S breakthrough occurs in effluent from first absorber 46. Preferably, the oxygen content and regeneration stream flow rate is established so that the regeneration time is about equal to absorption time prior to H2 S breakthrough. H2 S breakthrough can be determined by monitoring the H2 S content of the first absorber effluent stream 47 until H2 S content exceeds a predetermined limit. Following H2 S breakthrough, first absorber 46 can be placed on regeneration and second absorber 60 can be placed on absorption as described above.
While the invention has been described as required in accordance with a preferred embodiment and setting forth specific operating conditions and materials, the invention is not to be construed to be limited thereby but by the scope of the claims appended hereto.
|Cited Patent
|Filing date
|Publication date
|Feb 26, 1943
|Feb 18, 1947
|American Zinc Lead & Smelting
|Process of treating zinc oxides
|Dec 16, 1975
|Aug 23, 1977
|Institut Francais Du Petrole
|Process for purifying a gas containing sulfur compounds
|Aug 14, 1981
|Dec 14, 1982
|Institute Of Gas Technology
|Desulfurization of H2 S containing gas streams with production of elemental sulfur
|Oct 21, 1983
|Aug 6, 1985
|Standard Oil Company
|Sulfur recovery process
|Mar 8, 1985
|Oct 30, 1985
|Shell Internationale Research Maatschappij B.V.
|Process for the removal of sulphur compounds from off-gases
|Citing Patent
|Filing date
|Publication date
|Sep 9, 1996
|Jul 14, 1998
|Gas Research Institute
|Use of Z-Sorb process as catalytic incinerator for tail gas from sulfur plants
|Oct 18, 2011
|General Electric Company
|Methods and apparatus for reducing emissions in an integrated gasification combined cycle
|Sep 7, 2006
|Mar 13, 2008
|Terry Hughes
|Methods and apparatus for reducing emissions in an integrated gasification combined cycle
|Jan 14, 2005
|Apr 8, 2009
|Recovery of sulfur from a hydrogen sulfide containing gas
|Jan 16, 2004
|Jul 20, 2005
|Jacobs Nederland B.V.
|Recovery of sulfur from a hydrogen sulfide containing gas
|Jan 14, 2005
|Jul 28, 2005
|Jacobs Nederland B.V.
|Recovery of sulfur from a hydrogen sulfide containing gas
|Jan 14, 2005
|Nov 3, 2005
|Jacobs Nederland Bv
|Recovery of sulfur from a hydrogen sulfide containing gas
|U.S. Classification
|423/574.1, 423/230
|International Classification
|Cooperative Classification
|European Classification
|Oct 14, 1986
Owner name: AMOCO CORPORATION, CHICAGO, IL., A CORP OF IN.
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:MC GALLIARD, RUSSELL L.;REEL/FRAME:004627/0354
Effective date: 19860925
|Dec 26, 1991
|Fee payment
Year of fee payment: 4
|Mar 5, 1996
|Fee payment
Year of fee payment: 8
|Feb 28, 2000
|Fee payment
Year of fee payment: 12


text:
If you want to link to a website in France, you would need to get explicit permission from the rights holder", if two Parliament Members in France are successful in their proposal amendment.
The idea was proposed but rejected by the Legislative Commission, but it is brought back again. Socialist Karine Berger and Valérie Rabault once again tabled their Amendment #843 to Axelle Lemaire's Bill for a Digital Republic, which would actually prohibit by default a large quantity of hyperlinks in France.
This device aims at amending the Law for Confidence in the Digital Economy and hold ISP and hosts criminally responsible as soon as they "allow public access to works or objects protected by the copyright code, including through automated means."
The amendment states "users are required to obtain authorization from concerned rights holders". The two MPs demand that "such authorization covers actions by users of such services when transmitting to the said users the protected works or objects, in order to allow use as stated in the fist paragraph inasmuch as such users are not acting on professional purposes".
While it would be likely that website owners would have a blanket "everyone has permission to link to my site" for those sites in France, it becomes complicated when you consider the international scope of the web. Would website owners in France need to ask permission to link to sites outside of the country? And would websites outside of France need to ask permission to link to sites based in France? What about .fr sites that are hosted outside the country?
It does seem that it is another attack on Google, since they reference Google's linking practices specifically.
"Just look at Google's referencing procedures: they are based on hyperlinks, and links that lead to copyright-protected works on their publishing site are precisely what allows Google to create any added value whatsoever", said MP Karine Berger in her plea for the amendment.
"In other words, some commercial Internet operators benefit from the value of some copyright-protected cultural goods and services without ever paying for using them. The amendment, by raising the question as to whom is responsible for collecting value through hyperlinks, aims at overturning jurisprudence of the Court of Justice of the European Union. It is a paramount legal and economic issue."
Techdirt also confirms this opinion.
Similar to efforts in Germany, Spain and even the European Parliament, very, very shortsighted Google haters think that a way to "punish" Google is to make it pay money to sites that it links to (mainly when it comes to news aggregation). The two French politicians admit flat out that they're trying to help copyright maximalists.
But many site owners depend on traffic from Google that are outside of the realm of news. It doesn't seem to make any difference on the type of website, meaning it could prevent someone blogging from linking to a site they are a fan of or even product they like – something retailers would not be happy about.
France has been in the news more than once due to the way they want to govern the internet. They pushed for Google to remove all Right to be Forgotten removed results from all versions of Google, not just the EU versions. And France is also the country that wanted to force Google to reveal their entire search algorithm and to put 3 competitors, including a France-based competitor, on their homepage.
Jennifer Slegg
Latest posts by Jennifer Slegg (see all)
- Expanded Text Ads Now Available in Google AdWords - July 26, 2016
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- No PageRank Loss for 30x Redirects, Including 301 & 302 Redirects - July 26, 2016
- Sending Visitors Off Site Via Links Won't Hurt Site's Google Rankings - July 25, 2016
- Google AdWords Truncating Headlines for Some Ads - July 22, 2016

subset: commoncrawl


text:
Discussion BoardsOpen MenuDiscussion Boards Open Menu
BlogsOpen MenuBlogs Open MenuBeware of fake HP SupportOpen MenuBeware of fake HP Support Open MenuBe alert for scammers who may be posing as HP representatives and only call numbers from people who have a label next to their screen name. If you think you have received a fake HP Support message, please report it to us by clicking on the blue "Report Inappropriate Content" button above the message. Thank you!
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Message 1 of 2 (787 Views)
My SimplePass isnt working
I have a HP Envy Model: m6-1105dx which i just got yesterday and the SimplePass was working just fine yesterday.
Now it will only let me unlock my computer and thats it, it basically turns off after i unlock my computer.
A couple times it will say that it has stoped working i has to close it and after that it still wont come back on.
How can i fix this?
Regents Professor
Posts: 4,677
Member Since: 12-15-2011
Message 2 of 2 (772 Views)
Re: My SimplePass isnt working
Hello scrollofnevaeh,
Try to re-install it from the download here.
Let me know if this helps,
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11 July 2012|
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Unfourtunately some of the drams you selected for your are now out of stock :(
We've set your shipping destination to:
Prices vary based on delivery destination (it's a tax thing), so please change it if you're not shipping within United States as it might affect the price! (Why?)
The Islands represent a very diverse region and one that is not strictly recognised as a region by the Scotch Whisky Association - technically the Islands are a part of the Highlands. It is most probably for geographic ease that this small group of islands is lumped together. There are so many different characters to be found, although usually a slight salinity is to be found, thanks to the vicinity to the sea. To the very north there is Orkney, whose single malts are coastal and full in the case of Highland Park, with plenty of honey, malt and heather and smoky malt. The other Orcadian distillery, Scapa, has a delightful citrus and herbal quality. Then there is the Isle of Skye with its sole distillery: Talisker. Single malts here are often described as being 'volcanic' in character with plenty of body. There's Arran, who make a malty, rich whisky. It's a recently founded distillery on the Isle of Arran, founded in 1995. Finally, there's Mull and Jura. Each with a single distillery a piece. On Mull the Tobermory distillery produces a sweet, thick, slightly herbal whisky (and a heavily peated version called Ledaig) whilst on the Isle of Jura, the distillery with the same name produces some slightly maritime, oily drams with a nutty cereal character.
Ahh, Ledaig! A cracking single malt that proves Islay isn't the only place to get your hands on splendidly peaty whisky - the Tobermory distillers on the Isle of Mull also know their way around… More info
The 2010 release from Arran, the 14 year old replaces the previous benchmark, the 12. This was finished in fresh bourbon and sherry hogsheads 2 years before it was bottled. The result is a sweet,… More info
The Distillers Edition bottlings of Talisker single malt are allowed a finishing period in casks which have previously held wonderfully sweet Amoroso Sherry. This is the 2005 vintage, which has was… More info
The Isle Of Jura Turas-Mara was originally launched for the Travel Retail market, and is comprised of malts which have matured in a selection of different casks, including bourbon barrels, wine casks… More info
Jura's new 30 year old was nicknamed after the Standing Stone (the Carnas an Staca) - the name of the Isle of Jura's eight standing stones. These are the remains of an ancient stone circle which was… More info
A very special expression from Highland Park. Few distilleries have the requisite whisky stocks to add a 40 year old to the core of their range. Highland Park made sure this was sure to turn heads… More info
Ever tried a perfect whisky? Well this could be your chance! This bottling of 25 year old Highland Park single malt is made with whisky taken from ex-sherry and bourbon casks and bottled at 45.7%… More info
A very special whisky, bottled for the shareholders of the Isle of Arran distillery. The Founder's Reserve is light and gentle, and has notes of sweet, fresh apple. More info
You ever dram with the devil in the pale moonlight? Well, here's your second of three chances in this unholy trinity of releases.
Chapter II was created from 27 casks by Master Distiller James… More info
Matured in ex-bourbon barrels (various vintages) and finished for 18 months in American oak quarter casks for greater interaction. Bothy harks back to the 18th and 19th centuries on the Isle of Arran… More info
A bottle of Arran's excellent 10 year old single malt Scotch whisky complete with 2 handsome glasses! A gift pack to make anyone smile! More info
This was distilled at the Isle of Jura distillery in 1997 before a maturation in refill sherry hogsheads. This is a light, buttery whisky from Gordon and MacPhail's Connoisseurs Choice range. This… More info
A 2012 bottling of Talisker's 30 year old, massively satisfying single malt from the distillery on the Isle of Skye. Also, the box is jazzier than previous 30 year old releases! Nice! 3,186 bottles… More info
One of the more deluxe expressions from Highland Park's Warriors series, the Ragnvald was made using whiskies drawn mostly from European oak casks and a smattering of American oak casks. The name… More info
Many experts rate 21-year-old Highland Park as one of the best examples from this popular distillery. Originally created exclusively for global travel retail and duty free markets, this whisky was… More info
A 10 year old from the Tobermory distillery on Mull, a Gold Medal winner at the 2008 International Wine and Spirits Competition. More info
A 24 year old Highland Park finished for over three months in a tiny, specially rebuilt, fresh, first-fill 50 litre Pedro Ximénez Sherry cask! The small size of the cask creates greater interaction… More info
Elixirs are said to give life to those who need it, if fantasy fiction is to be believed. While we don't think this Isle of Jura 12 Year Old Elixir has any magical properties (in fact, we're sure of… More info
An indie bottling of Highland Park single malt, you say? Yes please! This is a Montgomerie's bottling of single malt Scotch whisky from the distillery on Orkney, matured in a single cask (#33, if you… More info
One of two inguinal release from The Library Collection, a series of independent bottlings from Edinburgh Whisky Ltd. This is a 15 year old Highland park, matured in a first fill bourbon barrel from… More info
You can spend years waiting for a new release in Talisker's core range then two come along at once! Hot on the heels of Talisker Storm in early 2013 comes Talisker's Port Ruighe, pronounced 'Port… More info
A superb 18 year old from the Highland Park distillery and a winner of a Gold Medal at the 2005 San Francisco World Spirits Competition. More info
A classic Island dram from the Isle of Skye. Always highly rated, this was an Editor's Choice at Whisky Magazine. Lots of spice and fresh, tangy peat. More info
A gentle, affable 10 year old single malt from the Tobermory distillery on the Isle of Mull. Now at the higher strength of 46.3%... More info
Officially launched in 2006, this 10 year old lies at the heart of the Isle of Arran range and exudes all the honeyed richness we have come to associate with the island distillery. More info


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Service and determines acceptability of service by reviewing picture. Performs service calls. Close vision, peripheral vision and ability to adjust....
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text:
UPDATE: Any moment now, it seems. ESPNNY.com's Katie Strang reports the New York Rangers have "zeroed in" on Alain Vigneault to replace John Tortorella as head coach. And the two sides are just a signed contract away from making it official.
Links from around the rink for April 20
461dDoug Mittler
Links from around the rink for April 6
475dDoug Mittler
Links from around the rink for March 23
489dDoug Mittler
What's next: Minnesota Wild
502dVictoria Matiash
What's next: Nashville Predators
502dVictoria Matiash
What's next: Arizona Coyotes
503dTim Kavanagh
What's next: San Jose Sharks
503dTim Kavanagh
What's next: Los Angeles Kings
503dTim Kavanagh
What's next: Colorado Avalanche
503dVictoria Matiash
What's next: Winnipeg Jets
503dVictoria Matiash
Links from around the rink - March 9
503dDoug Mittler
What's next: Dallas Stars
504dVictoria Matiash
What's next: St. Louis Blues
505dVictoria Matiash
What's next: Florida Panthers
505dVictoria Matiash
What's next: Calgary Flames
505dTim Kavanagh


text:
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"... our larger goal is to facilitate the world's first official, FIDE-certified online chess tournament." http://www.marketwire.com/press-release/World-Chess-Federation-Outlines-Big-Plans-for-Facebook-1296535.htm
Maybe Ilyumzhinov will elaborate here. http://www.facebook.com/people/Kirsan-Ilyumzhinov/100001218987074
looks interesting, but i stay away from facebook... so i'm out. To popularize chess, though, it makes sense.
w00t! Bad: Chess.com shall become swamped with social networkers Good: I'll get to play in a FIDE tourney for once! Small town blues. (Ignoring the fact I'll lose)
Problem is the use of chess engines during online play. They now have some software to detect heavy use of leaving page, computer trace etc but there are always holes in the system
And you think online cheating is bad now...
My Game Against a 124-rated player
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2826-4000 Worst Things To Do While Playing Chess
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Is this Magnus Carlsen?
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"Game Abandonded" While still playing
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Apart from boxing, what else would combine well with chess?
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Report Spam here! Spam Only! Not abuse, not cheating, Spam Only!
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#2672826, By Dracharon Sending an opened 360 back to MS
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10 Parks near Abilene, Kansas
Chapman, Kansas 11.21 miles NE
Junction City, Kansas 21.91 miles NE
803 S Buckeye Ave Abilene, Kansas 67410 (map) | (785) 263-2343
Sites: 60 | Latest Rate: $31.00 | 37 Reviews
|Clean Restrooms:
|Clean Showers:
Jul 2016 - $31.00
This is an overnight stay to visit Eisenhower's library and associated buildings. We got a pull-thru which suited our needs. Lots of trees and dirt driveways and pads. We had a picnic table. Arrived at 3 pm and found the office closed. Called the phone number on the door and someone came to check us in. On the main street and the occasional traffic noise was something to deal with. Staff was nice and helpful. Would stay again. - SD75mac
Jun 2016 - $32.00
We found this park by accident. Parks in nearby towns were full. I talked to the owner/manager on the phone to secure a site, but by the time we arrived the office was closed. I followed his instructions for after-hours checkin. There is good signage for entering and navigating through the park. Look for e right hand turn after entering to get to the bathhouse and office area. After-hours checkin is at the bathhouse. I found a long, level pull-through on the west side of the park, out of the heavily treed area, and didn't have to unhook our tow car. Most sites seemed to be long term residents, but the sites were all clean. Roads and sites were gravel and grass. There is a swimming pool and the site we were in had a picnic table. There is plenty of open area and dirt roads for walking dogs. The park is a few miles from the Interstate, accessed on the wide main road through town with lovely homes. There are nearby railroad tracks so we did hear trains periodically while there.
I would choose to visit again and take time to see some of the historic sites in town. - Dreaming
Nov 2015 - $33.00
We stayed only one night after visiting the Eisenhower Library and Museum which was just up the street about three blocks. The park was a little tight due to some trees between the street entrance and the overnighters' parking area. Otherwise we were satisfied with its value. - David_Leslie_JB
Abilene, Kansas (map) | (785) 598-2221
Sites: 87 | Latest Rate: $25.00 | 32 Reviews
|Clean Restrooms:
|Clean Showers:
Jul 2016 - $25.00
Lucky, although alot of sites didn't look that level: 74 isn't bad.
Lots of permanent residents but sites were clean. Most sites with shade are taken by residents. We had one tree that had very few leaves. Luckily it was cloudy and overcast. Would stay again to visit surrounding area. - Bill Dudley
May 2016 - $27.00
Nice overnight stay. Many seasonal people, but their rigs were quite new and everything was neat and tidy. Lots of grass with gravel sites. Average width of sites. We stayed in #22, which was perfectly level. There is a convenience store with pizza, wings, hot dogs and various sundries. The Shell station on the premises made it convenient to fill up and their price was great...$2.09 for diesel. Will stay again on our return trip. - lpampin
Mar 2016 - $25.00
Convenient stop along I-70. Facilities were clean and all worked, but need updating. A little paint and TLC would do wonders. Electrical pedestals need updating pretty badly.
Very nice convenience store folks. A gas station w/diesel if needed at competitive prices. - bobojay
2701 N. Marshall Chapman, Kansas 67431 (map) | (785)922-2267
Sites: 23 | Latest Rate: $32.00 | 10 Reviews
|Clean Restrooms:
|Clean Showers:
Jun 2016 - $32.00
Very nice. We have stayed here off and on all year and leave our camper in storage here most of the time. We feel very comfortable and welcome. They have the best camp hosts we have encountered. - d_h
Apr 2016 - $32.00
Great wifi, very clean bathrooms but... no privacy for dressing and undressing unless you literally stand in the shower stall. Had trouble getting water connected as we had to work around a rock down in the ground. Very difficult if you're handicapped. - Mrs.Picky
Mar 2016 - $32.00
Park is right off I-40, easy on/off. Pull through sites have some slope so I'm guessing these sites are better suited for 5th wheels than for motorhomes. There are two parallel pull through sites which are close to level. Backin sites look level. Staff is very helpful. Hookups/Wi-fi worked well. We camped here in a motorhome (in a parallel pull through) spot. - D-Lo
Junction City, Kansas (map) | (785) 238-5714
Sites: 66 | Latest Rate: $18.00 | 3 Reviews
|Clean Restrooms:
|Clean Showers:
Apr 2015 - $18.00
Traveling across country and needed an overnight spot. 11 miles north of I-70. Plenty of sites available on a weekday. We saw only 2 other trailers in "A" loop. There are restrooms throughout campground. Water and electricity at the sites, big rig friendly. Lots of space between the level gravel sites. Wide interior roads for easy backing into sites. Park like setting with trees and play area for kids. Great value if you have a National Park pass $9 per night. Normal rate is $18. Tent sites $12. This is a beautiful location a real gem! We camped in a 5th wheel. - Charlie M.
Sep 2013 - $9.00
Nice campground on Milford Lake. Our loop had only 30 amp and water, no sewer. There is a boat ramp nearby and some shady spots. Rate reflects Federal senior pass. Be advised that the campground is located 11 miles from the interstate. We were told that 50 amp sites are at another park. - lburas
Jul 2010 - $8.00
We have a Federal Parks pass, so rate was 1/2 off. There are only 5 sites with 50 amp, and is on a first come basis, no reservations. Sites are shady and there is a view of the lake from all sites. Will stay here again. Great value. Swim, fish and boat in the lake. Has boat dock. - dlbof
Junction City, Kansas (map) | (785) 238-5714
Sites: 56 | Latest Rate: $10.00 | 9 Reviews
|Clean Restrooms:
|Clean Showers:
Sep 2015 - $10.00
We were just needing a place to stay one night that wasn't too far off the hwy. and this was perfect, it was about 6 miles off of I-70 before Junction City, roads were a bit narrow but hardly any traffic. Stayed in A loop in space 6. It was a bit hairy trying to make the loop in our 38ft. class A. Other than that it was a beautiful place and quiet, we would come back and hopefully stay a little longer. - eagle94
May 2015 - $9.00
The park was difficult for our GPS to locate. There is no COE sign easily visible from Kansas Route 244, and K-244 was an unknown route to our updated Garmin. If this is your destination use coordinates 39.07681 and 96.92474. The park itself has lots of gravel sites in two loops. They offer water and electric with a dump & trash station at the entrance. We booked what appeared to be one of the last two sites available only to learn ( from a regular at this park ) that sites divisible by 3 ( 3 thru 15 and 16 ) cannot be reserved and are on a first come basis. At least two of these "open" sites would have served us better than the one we reserved as far as satellite reception was concerned. We also learned that nobody patrols this facility as evidenced by trash in our fire pit and loud music from a site a few hundred yards away. The closest eating/shopping is at least 5 miles away and the better places are on Ft. Riley, which is open only to the military or retirees. The closest bath house did not include any shower facility. Our Verizon cell and the associated hot spot allowed us access to the internet. They close and lock the campground gates at 10 PM and open at 7 AM. Sites 1-16 in Loop A offer 50 amp, all other sites are 30 amp only. They offer a tenting area and a separate fish clean station near the park entrance. This is probably a boating and fishing paradise - especially here in Kansas. The Golden Age/Senior Pass discounted our site to 9.00 per night. - 5thwheeler
May 2015 - $10.00
Nice sites, lake views, close to the water. We will probably return. - Oldtymeflyr
Junction City, Kansas (map) | (785) 238-0778
Sites: 29 | Latest Rate: $32.00 | 22 Reviews
|Clean Restrooms:
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Apr 2016 - $32.00
We needed an overnight stop near Manhattan, KS, to visit friends and chose this campground based on previous recommendations. When I called to make reservations, I told the campground attendant that we were a 40' motorhome towing a full-sized pickup, and wanted to be sure that this campground could accommodate us. No problem, I was told! Imagine our surprise when we pulled into this teeny place and could barely negotiate the fairways with our pickup unhooked! We were in site 11, right next to the road, and got to hear the early morning workers headed to their jobs. I-40, indeed, was only 1/2 mile away, adding to the noise. Yes, they do have cable, but we needed a "box" to access their service. Rather out-dated. We will never stay here again. - JanW
Jul 2015 - $32.00
Needed a place just overnight while traveling through. What a nice find. Place is half mile off the highway, flat, and easy to navigate even at night. Almost all sights are pull through and easily accommodated my 40' RV. Folks were nice and I will use again when in the area. - colotiger
May 2015 - $32.00
Very nice park. Good central location. Good management. Only one shower. - d_h
Milford, Kansas (map) | (785) 238-3014
Sites: 141 | Latest Rate: $20.00 | 7 Reviews
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Jul 2016 - $20.00
We stayed here rather than a parking lot on our trip across Kansas going to Colorado. What a lovely surprise. Largest lake in Kansas. We didn't do anything in the park but you could spend a weekend here. The parking sites were wonderful. Ours was a pull through with an obstructed view of the lake. Concrete level pad with full hookups. Well worth the drive off the interstate. - RosalitaAS
Jul 2015 - $24.00
The site was near the water and had amazing views, but the night-time bugs were horrible. I would not open the door after dark. Several pull through sites are one-way on a single lane road section. The last person in has to wait for the previous one to leave, or break the rules and drive through the grass. See the camp host before picking your site, they live a long ways away from the camp sites. - Keystone Trail
Jul 2015 - $28.00
Review applies only to a five night stay in the Eagle Ridge section (equestrian loop); other loops vary greatly in character and services. Easy access to and in the park with our oversized 40'+ BigRig RV. Price paid includes a daily vehicle fee that wasn't mentioned until check-in. Poorly designed loops; park has plenty of space but many sites are very close to one another and many with oddly placed utility services - choose a suitable site carefully ahead of time if making reservations. Would have rated park lower but it was very quiet at night. We would stay again but certainly wouldn't go out of our way to do so. - Snidely Whiplash
Salina, Kansas (map) | (785) 827-3182
Sites: 95 | Latest Rate: $55.00 | 128 Reviews
|Clean Restrooms:
|Clean Showers:
Jul 2016 - $55.00
We stayed in a 40' class A motorhome with no slides There are lots of large trees on this property and one must be careful navigating. We pulled in OK but had to back out to leave due to tree placement. I love trees but it wins against a motor coach.
Be careful about specifying and understanding the electrical service layout. Adjacent sites are designated 30 and 50 amp and are served out of the same electrical box. We tried and failed to use the 30 amp service as the 50 amp was in use by the 30 amp site. We had to relocate at managements request.
The setting is pretty with minimal noise from the freeway. - Travelall
Jul 2016 - $31.00
Not sure on the price but it was around $31. The site was OK with some sun. We arrived early in the afternoon with the temperature around 93 and a heat advisory in effect. As the park started filling around 5:30 pm we had our first power failure. The camper next ours immediately went to the office and was told they would check on it. The power came back on a few minutes later. Someone from the office came by and said they had someone on the way to check it out but I never heard back from them. The park was full that night and we had several more brief outages. This didn't make for a very pleasant night with temperatures this hot. I don't know if everyone was impacted or just those around on our row. It is an older park and I don't know if the infrastructure was over loaded or the problem was with the power company. - NEOK
Jul 2016 - $36.00
Easy to get to from the interstate. we were at the back, so highway noise was minimal. But the Birds in this park make it noisy, and they get up early! Concrete pad was narrow and the grass was muddy from Rv traffic. It was difficult to find a dry spot to have in front of your door. The phone staff were a little inexperienced, and others a bit gruff. - acadiandave
Junction City, Kansas (map) | (785) 463-5791
Sites: 59 | Latest Rate: $10.00 | 5 Reviews
|Clean Restrooms:
|Clean Showers:
Aug 2015 - $10.00
This campground is nice if you like fishing and boating in a small lake, little else to do in the area. The biggest problem is that they only have one handicapped site and that cannot be reserved but rather, on a first come first served and no requirement to be handicapped to get this site. So if you are handicapped this isn't a great park. - dlbof
Jul 2015 - $10.00
Nice views, but service was bad. We are handicapped and were told we couldn't have a handicapped site, because it was taken. The folks staying in the handicapped stall were not handicapped. It appears that every rule for COE parks are violated. Folks freely empty their holding tanks, dogs are not leashed, campers were parked and left vacant during the week, with occupants coming in for week-ends, trailers with boats and cars parked on the grass. No one manning the booths during the day, so it is hard to check in. We do like the park, but the contract people are not competent. The volunteers were not helpful. - eileenb
May 2012 - $9.00
We used our National Park discount for the 1/2 price ($18 a night regular price) - stayed 2 nights. It was a wonderful, peaceful campground near a beautiful lake. We enjoyed our 2 night stay. Visited Junction City WalMart (very nice) to stock up. No 10 since it didn't have sewer. We enjoyed the park and would visit there again if we were in the area. Park has 4 showers near the entrance of the park. The bathrooms are clean and placed around the park. The hosts are very helpful. Lots of boats and great fishing apparently in the area. Located near Junction City on one of the state's largest lakes. Campsites located right on the lake if wanted. One loop has no facilities. - westie0506
Milford, Kansas (map) | (785) 463-5537
Sites: 260 | Latest Rate: $25.00 | 1 Reviews
|Clean Restrooms:
|Clean Showers:
Oct 2010 - $25.00
We usually don't have a problem finding our way to a 'new-to-us' campground; but this time we did. When you are going north on highway 77 and looking for where to turn left, the Flagstop Resort sign is on the right side of the highway but it is located past where you actually make the turn. Plus, if sunlight is reflecting off the sign, it is very hard to read. So when you see the green highway sign that points to the left and says 'Milford', turn there. After that, there is not another sign that says 'Flagstop' until you reach the entrance. You will need to watch for one of those small, square signs with a trailer on it so you know where to make the next left into the neighborhood. There is only one entrance and one exit. This campground caters to seasonal tenants. A lot of the sites have a rig and a boat plus an abundance of 'stuff' outside. We encountered low hanging trees and large speed bumps. There are some side by side hookups which puts you very close to your neighbor. We were in a full service site at the end of a row and enjoyed our view of the city park. Our site was level, hard-packed dirt, but not all sites looked at good as this one. The services all worked well. We would stay again if we got this same site. - B&H


text:
WHAT: Silent Night, Winter Light, a Winter Wunderland Holiday Concert presented by the University of North Dakota Department of Music
WHEN: November 30, 2012 at 8:00 pm
WHERE: Chester Fritz Auditorium
TICKETS: Chester Fritz Box office 701-777-4090, at Ticketmaster.com, or at the door. $12 General Admission.
INFORMATION: Dr. Joshua Bronfman, firstname.lastname@example.com, 701-777-2814.
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Watch Featured Movies
Psych: A novice sleuth (Roday) is hired by the police after he cons them into thinking he has psychic powers that help solve crimes. With this assistance of his reluctant best friend (Hill) the duo take on a series of complicated cases.
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Season seven starts February 27, 2013
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Best show ever. Funny, crime solving...just simply excellent. WHY?! Why must this wonderful show end. (Sigh.) It's really sad.
|Posted by pinkgirlx3 2 years, 4 months ago
R.I.P. Psych... This was one of my favorites.
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It's so stupid, but they were really part of my family. Get that, a show that you just want to step in. I'll miss them, but no worry, still see 1 every day, just to keep smiling at the end of the day!
|Posted by provostg 4 years, 11 months ago
Hey did you guys know James Roday and Maggie Lawson have been together since 2006?
|Posted by ImagineCrazy 1 year, 2 months ago
One of my favourites! And I believe Shawn and Juliette are dating in real life!?
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My favorite buddy show. I can watch this all day.
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so sad this show ended one of the best detective crime solving comedy ever i really loved this show
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Great show, if you're thinking of watching, do already! It's an amazing show and you wont regret it. 9.5/10!
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So funny, smart and awesome - just saw episode 1 and I'm pretty much hooked.
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the show has always been funny, but now the plots are getting better!
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They have definitely upgraded the quality of this show since I last watched it. Nice!
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one of my favorite shows, i wish they could make more shows like this :)
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This is very funny for me, being that I live in Santa Barbara, you see all the over head shots but the street shots are not in Santa Barbara.
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How amazingly fun would it be to on the cast of this show. Jealous, so very jealous.
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Just two more days...YAY!!! Wednesday Oct. 12th
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It's an amazing show and you wont regret it.
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I really really love this show.It's just too bad that they're not doing the kids Shawn and Kid Gus flash backs anymore:(
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February 27, 2013 season 7 starts
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healthcare professionals network: community health services Innovative community health services help ease the pressure on GPsNew models of care for the growing number of people with long-term health issues are being offered around the country
With money for basic and clinical research squeezed, some health researchers – including the UK team behind a dementia drug – are trying crowdfunding
Drug development is highly resource-intensive and expensive with only one in 5,000 medicines making it to the market – this is how it works
We can all point to examples of good practice, but we must ask whether we are doing enough to scale up what works
Manchester Camerata orchestra is pioneering music projects in care homes; now academics are to study whether the sessions do more than just entertain participants
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Laramie News
Local news for Laramie, WY continually updated from thousands of sources on the web.
Fracking: Progress or Poison?
Iran Nuclear Agreement: Black Mark or Gold Star for Obama?
Tragic: 40 Stars Who Committed Suicide
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Updated: Sun Jul 24, 2016 05:51 pm
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