• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The method of and a device for conditioning sludges, especially sewage sludges at an increased pressure and at an increased temperature wherein the raw sludge is fed by means of high-pressure pumps through a plurality of heat exchanging stations until it is brought in the last station to a pressure which is sufficient for the conditioning. Thereupon the conditioned sludge is returned through the same stations and in each station is pressure released and cooled. Steam released due to the cooling is brought in contact with the incoming raw sludge and warms up the same to a saturation temperature. To insure optimum heat exchange, each station is provided with means for measuring the concentration of gas components admixed to the steam and the discharge of the gaseous mixture from the station is controlled in response to the measured concentration value.
    公开号:SU833154A3
    申请号:SU792744252
    申请日:1979-04-04
    公开日:1981-05-23
    发明作者:Коглин Бодо
    申请人:Ферайнигте Кессельверке (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a method for the continuous conditioning of sludge, in particular sewage sludge at elevated temperatures and pressures, and can be used in wastewater treatment plants.
    A known method of regulating the process of heat treatment of sludge by removing gas from the reactor depending on its pressure in the upper part of the reactor and the supply of coolant depending on the temperature of the sludge in the reactor [1].
    The closest in technical essence to the invention is a spo- 'GSS regulation schlama heat treatment process, wherein the pressure set in separate steps using gazospusknyh valves, _ wherein the first at a given base 20 to the reactor pressure, wherein the conditioning takes place, determine the optimal pressure of the individual stages inappropriately, 25 set the valves so that when the calculated pressure is exceeded, the corresponding amount of gas is released [2].
    However, if for any reason it is advisable to change the pressure of both the reactor and the pressure, the pressures must also be changed at different stages of heat transfer. Pressure deviations at which the pressure is below the calculated optimum pressure cannot be counteracted. To adjust these pressures, additional techniques are needed, such as blowing steam into the appropriate stage. But this requires additional investment and production costs. Also, the descent of gas from the intermediate stages is always associated with heat loss and therefore should be limited to a minimum. But, a certain descent of the gas is necessary, since the atmosphere in separate steps, which in the ideal case should consist of pure water vapor, is actually enriched with a more or less inert gas, primarily carbon dioxide, while an inert gas impairs heat transfer.
    The purpose of the invention is to reduce heat loss.
    This goal is achieved by the fact that the discharge of the exhaust gas is changed depending on the concentration of inert gas in the reactor and heat exchangers, and the concentration of inert gas is determined by the temperature difference of the crude and depleted sludge.
    The formation of inert gas in the individual steps is different. This formation is especially noted, first of all, in the coldest and hottest steps. In the middle steps, on the contrary, no inert gas appears. In accordance with this, with the proposed 'regulation method, heat losses in the medium and their levels can be almost completely avoided.
    For each stage, the difference between the temperature at the outlet of the raw sludge and the temperature at the outlet of the conditioned sludge is a measure of the concentration of inert gas. This is acceptable, since the indicated difference in temperature is a consequence of imperfection of heat exchange, which is primarily due to the inert gas content.
    In FIG. 1 shows a diagram of an air conditioning installation; in FIG. 2 is a control diagram of a direct heat exchanger.
    Installation 1 includes three direct heat exchangers 2-4. However, in practice, as a rule, there is a larger number of direct heat exchangers up to about six - as optimal. Direct heat exchangers consist of straight cylindrical tanks with concave bottoms. Each direct heat exchanger is divided by inclined horizontal partitions 5-7 into the lower 8-10 and upper 11-13 chambers. Through the intermediate holes re-. 5 town cameras communicated with each other. Pipes 14-16, welded with the edges of the holes, extend from the horizontal partitions up. Between these partitions and the outer walls of the 40 straight heat exchangers there are annular grooves above the partitions. In chambers 11-13, cascading shields 17-19 are located.
    The untreated sludge from the reservoir 45 (not shown) goes through the pipeline '20 through the high pressure pump 21 to the upper bottom of the direct heat exchanger 3, which it passes in the middle. The corresponding pipelines jq 22 and 23, each of which has a pump 24 and 25, exit the channels 26 of direct heat exchangers 4 and 3 and are connected to subsequent direct heat exchangers 3 and 2. ..
    A pipe 27 is provided with a pump 28, which exits from the chute of the direct heat exchanger 2 and enters the reactor 29 from above.
    The reactor 29 in its upper part is also equipped with cascade guards 60 30. A conduit 31 for supplying extraneous steam is connected under the cascade guards.
    From the bottom of the reactor 29 there is a pipe 32 containing a valve 65 to reduce pressure, and enters from the sides into the chamber 8 of the direct heat exchanger 2. Corresponding connecting pipelines 34 and 35 with valves 3.6 and 37 connect adjacent, direct heat exchangers. From a direct heat exchanger 4, a pipe 38 with a valve 39 exits.
    Gas pipelines 40-43, equipped with valves 44-47, are connected to the upper part of the reactor 29 and direct heat exchangers 2-4 and are connected to the collector 48.
    The method is as follows.
    The untreated sludge is pumped through a pipe 20 into the chamber 13 of the direct heat exchanger 4, where it, when it enters the cascade guards 19, is distributed and heated by the heat of condensation from the vapor leaving the chamber 1.0. The heated crude sludge with evaporated condensate forms a collector in the trough 26 and is pumped out from there by a pump 24 through a pipe 22 at an increased pressure to the next direct heat exchanger 3. In this and the next direct heat exchanger 2, the described process is repeated. The raw sludge heated in this way is brought by the pump 25 to the pressure of the reactor and pressed into it. There, it flows down with a thin stream-shroud down the cascade shields and, by direct heat exchange, is brought by the on-going exhaust gas and extraneous steam supplied through the pipeline 31 to the temperature of the reactor. After the necessary time spent in the reactor of the raw sludge fed from above, the conditioned sludge already leaves the bottom through the pipe 32 from the reactor and the pressure in the pressure reducing valve decreases to the pressure present in the direct heat exchanger 2. In this case, the conditioned sludge is cooled by evaporation. In the chamber 8 of the direct heat exchanger, the conditioned sludge and steam are separated from each other. Vapors rise into chamber 11 and mix there with less hot, untreated sludge. The conditioned sludge forms a collector on the bottom, from which it flows through line 24, after which pressure in the expansion valve 36 decreases again. In direct heat exchangers 3 and 4, the corresponding process occurs and a much chilled, conditioned sludge then leaves through the pipe 35 from the device.
    Each direct heat exchanger in the upper and lower collectors has one thermocouple 49 and 50, from which one continuously measures the temperature of untreated sludge flowing in the direction of reactor 29, and the other continuously measures the temperature of the outgoing conditioned sludge. Thermocouples 49 and 50 are switched on with an opposing sequence one against the other, the resulting voltage difference is converted by the measured value converter 51 into an electrical signal 3 . This signal is supplied for further processing to the controller 52. If a deviation from the set set value occurs, the controller 52 gives an output signal corresponding to this deviation 10 in the form of an electric signal to the electromagnetic signal converter 53. This converter converts the electrical signal into a hydraulic signal 15, which is then fed to the pneumatic positioner 54. This controller provides, using the pneumatic actuator 55, the position of the valve 45. Corresponding to the 20 output signal of the controller 52.
    The pressure of the regulator is regulated by · the supplied foreign steam. Due to the inert gas participation, the temperature of the sludge in the reactor 25 is several degrees lower than the saturation temperature. The sludge temperature is controlled by the fact that the corresponding amount of exhaust gas is discharged through the valve 44. So much gas is discharged from the individual direct heat exchangers 2-4 with the help of a regulating device that the difference in temperature, which in the absence of inert gas during complete heat transfer would be - very small, not, exceeds the specified maximum value. This means that the inert gas concentration is kept so low that it does not impair heat transfer beyond the inevitable, but possibly .40, small size. Thus, in direct heat exchangers 2-4, the pressure and temperature are automatically set to optimal intermediate values so that a stepwise increase is created for 45 incoming untreated sludge, and a stepwise decrease in pressure and temperature for flowing conditioned sludge.
    The difference in temperature is only a measure or indicator of the presence of inert gas. Inert gas is the main reason for the deterioration of heat transfer. Therefore, in another embodiment of the proposed method, the concentration of inert gases is used as an adjustable quantity. Of course, among individual direct heat exchangers it is not constant, but increases from bottom to top. Therefore, it is the largest in the exhaust gas and is measured there. Moreover, the moisture content is determined for the entire exhaust gas stream of each direct heat exchanger or for one of the partial flow branched from it.
    The remainder is an inert gas. Regulation is taking place. accordingly (Fig. 2) only with the difference that instead of the difference in temperature, the concentration of the inert gas serves as an adjustable value.
    权利要求:
    Claims (2)
    [1]
    .,. -. k -, The invention relates to a method for continuous conditioning of sludge, in particular sewage sludge at elevated temperature and elevated pressure, and can be used in sewage treatment plants. There is a method of regulating the heat treatment process of sludge by removing the gas from the reactor, depending on its pressure in the upper part of the reactor and the supply of coolant, depending on the temperature of the sludge in reactor 1. The closest to the technical essence of the invention is a method for regulating the heat treatment process of sludge, in which the pressure is set in separate stages by means of gas release valves, first of all determining the optimal conditions on the bases of a given pressure for the reactor in which conditioning takes place. pressures of individual stages and, accordingly, install valves in such a way that when the calculated pressure is exceeded, the corresponding amount of gas goes down 12}. However, if for some reason it would be advisable to change the pressure of the reactor, this should also change the pressure in the various heat exchange stages. Deviations of pressure at which the pressure is below the calculated optimal pressure cannot be counteracted. To adjust these pressures, additional techniques are needed, such as, for example, blowing steam into the appropriate stage. But this requires additional investment and production costs. Also, the release of gas from the intermediate stages is always associated with heat loss and therefore should be limited to a minimum. But, a certain gas release is non-. This is due to the fact that the atmosphere in individual stages, which in the ideal case should consist of pure water vapor, is in fact enriched with a more or less inert gas, primarily carbon dioxide, and the inert gas impairs heat transfer. The purpose of the invention is to reduce heat loss. This goal is achieved by the fact that the exhaust gas exhaust is changed depending on the concentration of inert gas in the reactor and heat exchangers, and the concentration of inert gas is determined by the temperature difference between the crude and purified ishams. The formation of inert gas in the individual stages is different. This formation is especially marked, first of all, in the most cold and in the hottest steps. In the middle stages, on the contrary, no inert gas appears, in accordance with which, with the proposed control method, heat loss can be almost completely avoided in the middle stages. For each stage, the difference between the temperature at the outlet of the crude sludge and the temperature at the outlet of the conditioned sludge is a measure for the concentration of inert gas. This is acceptable, since this temperature difference is a consequence of the imperfect heat exchange, which is primarily due to the inert gas. FIG. 1 shows the layout of the power installation; in fig. 2 - direct heat exchanger control circuit. Installation 1 includes three direct heat exchangers 2-4. However, in practice, as a rule, there are more than about six direct heat exchangers - how optimal the direct heat exchangers consist of straight cylindrical tanks with concave bottoms. Each direct heat exchanger is divided by inclined horizontal partitions 5–7 into the lower 8–10 and Hci upper 11–13 chambers. Through the holes of the intermediate partitions of the chamber communicated with each other. Tubes 14-16, welded to the edges of the holes, extend from the grrisotal partitions upwards. Between these walls and the outer walls of the heat exchangers there are annular grooves above the partitions. In the chambers 11-13, cascade flaps 17-19 are located. Crude sludge from a tank (not shown) flows through conduit 20 through a high-pressure pump 21 to the upper bottom of the direct heat exchanger 3, which it passes through the middle. The respective pipelines 22 and 23, each of which has a pump 24 and 25, come out of the grooves 26 of the direct heat exchangers 4 and 3 and are connected to the subsequent direct heat exchangers 3 and 2. There is a pipeline 27 with the pump 28, which comes out of the groove My heat exchanger 2 and enters the reactor 29 from above. The reactor 29 in its upper part is also equipped with cascade flaps 30. A pipeline 31 is connected under the cascade flaps for supplying extraneous steam. From the bottom of the reactor 29 there is a pipe 32 containing a valve 33 for reducing pressure, and enters from the sides into the chamber 8 of the direct heat exchanger 2. Corresponding connecting pipes 34 and 35 to the valves 36 and 37 are connected to the adjacent, direct heat exchangers . From the direct heat exchanger 4, a pipeline 38 with a valve 39 comes out. Gas supply pipes 40-43, equipped with valves 44-47, are connected to the upper part of the reactor 29 and direct heat exchangers 2-4 and are connected to the collector 48. The method is as follows. Crude sludge is supplied by pump 21 through conduit 20 to chamber 13 of the direct heat exchanger 4, where it is distributed and heated with condensation heat from the vapor chamber 10 when it enters the cascade flaps 19. The heated raw sludge with evaporation condensate forms a collector in chutes 26 and is pumped out from there by pump 24 through conduit 22 at pressurized pressure to the next direct heat exchanger 3, In this and the next direct heat exchanger 2, the described process is repeated. The raw sludge thus heated is brought by pump 25 to the pressure of the reactor and pressed into it. There, it flows down in a thin stream-shroud on the cascade shields downwards, and at the same time, by direct heat exchange, it is brought to the temperature of the reactor by counterflow exhaust gas and 31 supplied through the pipeline 31 with extraneous steam. After the required residence time in the reactor of the raw sludge fed from above, the conditioned hose already exits from the bottom through conduit 32 from the reactor and in the redox valve the pressure is reduced to the pressure in the direct heat exchanger 2. The conditioned slurry is cooled during evaporation. In the chamber 8 of the forward heat exchanger, the conditioned sludge and steam are separated from each other. Spars are lifted into the chamber 11 and mixed there with less hot uncleaned sludge. The conditioned slurry forms a collector on the bottom, from which it flows through conduit 24, then in the expansion valve 36, the pressure decreases again. In direct heat exchangers 3 and 4, an appropriate process takes place and, much cooled, the conditioned sludge leaves then through conduit 35 from the device. Each direct heat exchanger in the upper and lower collector has one thermoelement 49 and 50, from which one measures continuously the temperature of the crude sludge flowing in the direction of the reactor 29, and the other is continuously measured. The temperature of the output of the conditioned slurry. Thermocouples 49 and 50 are turned on with a counter-sequence one against the other, creating as a result the difference in voltage is converted by the converter 51 of a measured value into an electrical signal. This signal is fed for further processing to the controller 52. If a deviation from the setpoint is set, the controller 52 provides the output signal in the form of an electrical signal to the electromagnetic signal converter 53 corresponding to this deviation. This converter converts the electrical signal into a hydraulic signal that is fed further to the pneumatic position controller 34. This regulator provides the position of the valve 45 with the help of a pneumatic servo drive 5., corresponding to the output signal of the regulator 52. The regulator pressure is regulated. . Due to the share of inert gas, the slurry temperature in the reactor is several degrees below the saturation temperature. The temperature of the sludge is controlled by the fact that the corresponding amount of exhaust gases is lowered through the valve 44. So much gas is lowered from the individual direct heat exchangers 2-4 using a regulating device that the difference in temperature which in the absence of inert gas would be completely insignificant effective, does not exceed the specified maximum value. This means that the concentration of inert gas is kept so low that it does not impair heat transfer beyond the Inevitable, but possibly of insignificant size. Thus, in direct heat exchangers 2-4, pressure and temperature are automatically set to optimal intermediate values so that a stepped increase is created for the incoming raw sludge, and a stepped decrease in pressure and temperature for the flowing down conditioned slurry. The difference in temperature is only a ker or an indicator of the presence of an inert gas. Inert gas is a major cause of heat transfer deterioration. Therefore, in another embodiment of the proposed method, the concentration of inert gases is used as an adjustable value. Of course, among the individual direct heat exchangers, it is not constant, but increases from bottom to top. Therefore, it is greatest in the exhaust gas and measured there. At the same time, the moisture content is determined for the entire exhaust gas flow of each direct heat exchanger or for one of the partial branch streams from it. The residue is an inert gas. Regulation takes place accordingly (Fig. 2) only about the difference that instead of the difference in temperature, the concentration of inert gas serves as an adjustable value. Claims 1. Process control method. heat treatment of the sludge by changing the exhaust gas from the reactor and heat exchangers, characterized in that, in order to reduce heat loss by increasing the control accuracy, the exhaust gas exhaust is changed depending on the concentration of inert gas in these devices .. 2. Method according to claim 1, distinguishing U and in that the concentration of inert gas is determined from the temperature difference between the crude and purified sludges. Sources of information taken into account in examination 1, UK Patent No. 1379929, cl. C 1 C, 1975.
    [2]
    2. The patent of Germany No. 2019731, cl. From 02 to 3/00, 1974.
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    同族专利:
    公开号 | 公开日
    DE2826132B1|1979-07-19|
    DE2826132C2|1980-03-27|
    SE7902161L|1979-12-16|
    JPS553895A|1980-01-11|
    US4261836A|1981-04-14|
    GB2023117B|1982-08-25|
    SE432924B|1984-04-30|
    GB2023117A|1979-12-28|
    BR7903487A|1980-01-22|
    FR2428614A1|1980-01-11|
    FR2428614B1|1983-04-29|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    GB1053249A|1962-10-18|
    US3272740A|1964-06-24|1966-09-13|Sterling Drug Inc|Sewage sludge treatment process|
    GB1185163A|1966-05-24|1970-03-25|Norstel And Templewood Hawksle|Improvements in or Relating to the Treatment of Sewage and Other Organic Sludges|
    DE2019731C3|1970-04-20|1974-11-21|Ver Kesselwerke Ag|Process for treating sewage sludge to improve its drainage properties and device for carrying out the process|
    US3661778A|1971-01-18|1972-05-09|Sterling Drug Inc|Wet air oxidization system for strong sludges and liquors|
    DE2137453C3|1971-07-27|1980-07-03|Vereinigte Kesselwerke Ag, 4000 Duesseldorf|Methods and devices for the treatment of sewage sludge|
    US3804755A|1971-08-02|1974-04-16|L Cervantes|Sewage treatment system|
    US3986955A|1975-01-28|1976-10-19|Sphere, Incorporated|Effluent waste treatment process and apparatus|
    US4013560A|1975-04-21|1977-03-22|Sterling Drug Inc.|Energy production of wet oxidation systems|
    US4100730A|1975-06-04|1978-07-18|Sterling Drug, Inc.|Regulation of a wet air oxidation unit for production of useful energy|AT14081T|1980-12-06|1985-07-15|Wool Dev Int|WASTE ORDER.|
    EP0289057B1|1987-05-01|1991-06-12|Limus Umwelttechnik Gmbh|Process and apparatus for the treatment of digested sewage sludge|
    JPH0243999A|1988-06-16|1990-02-14|Shell Internatl Res Maatschappij Bv|Medium temp. hydrolysis reactor|
    US5593591A|1995-06-07|1997-01-14|Unipure Corporation|Production of dry, free flowing solids from bio-waste sludge|
    US6013183A|1998-08-05|2000-01-11|Paradigm Environmental Technologies Inc.|Method of liquefying microorganisms derived from biological wastewater treatment processes|
    US6372085B1|1998-12-18|2002-04-16|Kimberly-Clark Worldwide, Inc.|Recovery of fibers from a fiber processing waste sludge|
    DE19940994B4|1999-08-28|2004-02-26|Clausthaler Umwelttechnikinstitut Gmbh, |Process for the removal of sewage sludge|
    DE10014185A1|2000-03-23|2001-09-27|Bsbg Bremer Sonderabfall Berat|Hot, high pressure ammonia treatment for excess sewage sludge, subsequently reduces pressure by expansion and recycles steam to heat feedstock|
    FR2820735B1|2001-02-14|2004-05-14|Vivendi Water Systems|PROCESS AND PLANT FOR THE THERMAL HYDROLYSIS OF SLUDGE|
    US7364642B2|2003-08-18|2008-04-29|Kimberly-Clark Worldwide, Inc.|Recycling of latex-containing broke|
    GB2452071A|2007-08-24|2009-02-25|Willacy Oil Services Ltd|An apparatus for treating sediment|
    NO330122B1|2009-07-13|2011-02-21|Cambi As|Process and apparatus for thermal hydrolysis of biomass and steam explosion of biomass|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2826132A|DE2826132C2|1978-06-15|1978-06-15|Process for the continuous conditioning of sludge|
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