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    • 专利摘要:
    method and installation for drying paste-like materials, in particular sludge from waste water treatment facilities. the invention relates to a method for drying paste-like materials, in particular sludge from waste water treatment facilities, including two drying stages, namely: a first indirect drying stage (2), supplied with fluid hot, which receives the sludge having a degree of dryness inlet, and sends the sludge having an intermediate degree of dryness itself and water vapor, which is channeled towards a condenser (8) where a heating fluid, in particular water, is reheated and, in turn, heats a heating gauze to a second drying stage (6); and a step (5) of formation of mud threads at the exit of the first stage; the second stage (6) for drying mud strands using gas at least partially heated by the heat extracted from the condenser, said second stage sending a paste having a final dryness degree sf; the degree of intermediate dryness itself being controlled according to the degree of dryness measured if and the degree of desired dryness sf for a minimum consumption of the total energy used to dry, the flow rate, pressure and / or temperature of the hot fluid (3) supplied the first drying stage (2) being adjusted accordingly.
    公开号:BR112012012380B1
    申请号:R112012012380-7
    申请日:2010-11-19
    公开日:2020-09-15
    发明作者:Pierre Emmanuel Pardo
    申请人:Degremont；
    IPC主号:
    专利说明:

    [0001] The present invention relates to a method of thermal drying of paste-like materials, in particular sludge obtained from waste water treatment facilities, with a very low consumption of thermal energy.
    [0002] The present invention can be used for drying any paste system to be dried, and which, in a pre-dried form, can be placed in the form of spaghetti-like threads.
    [0003] The technique for thermal drying of sludge obtained from urban wastewater treatment facilities is well known: there are different technologies that make it possible to obtain a finished product, the final drying of which is 85% or more .
    [0004] The main objection to thermal drying is the use of excessively high energy that is required for that drying, and therefore the resulting operating costs.
    [0005] This is why, in certain belt drying methods, thermal drying in order to dry the paste can recover calories and a low temperature (50 - 90 C), which is the dead heat and therefore not used by another process (joint generation, turbine condensation, heating pump, solar thermal system, biogas heater, etc.). However, this dead heat is generally insufficient to dry the sludge completely. This results in substantial energy consumption.
    [0006] Additionally, these belt drying technologies with low temperatures cannot be used to dry the sludge that is not sufficiently dewatered upstream, since it is not possible to spread a spaghetti mat satisfactorily through the dryer.
    [0007] In other methods, thermal drying recovers heat from the drying process itself, but this circuit is not optimized from an energy point of view.
    [0008] The dryers that currently exist have an energy required for drying the sludge of approximately 900-1100 kWh / TEE (Ton of Evaporated Water). These dryers can be direct dryers, according to which the hot drying fluid, which is generally a gas, is directly in contact with the sludge to be dried, or indirectly, according to which the hot gas or Drying liquid transmits its heat to the mud through a wall.
    [0009] The degree of dryness of a sludge can be defined as the ratio of the mass of dry substances (DM) to the total mass of the sludge (MS + water), that is, MS / (MS + H2O).
    [0010] EP 0 781 741 B1 describes a method for drying paste-like products, in particular sludge from waste water treatment facilities, of the type comprising: a first drying stage (indirect drying) which receives the sludge with an input dryness degree Se, and sends the sludge with an intermediate dryness degree Si; a stage of formation of mud threads leaving the first stage; and a second stage of direct drying of the mud strands by means of a hot gas that releases a product that has a final dryness Sf.
    [0011] Such drying methods and drying systems with sludge pre-evaporation can obtain energy consumption of 700 - 800 kWh / TEE. This energy consumption is optimized in comparison with the dryers initially mentioned, since the reuse of part of the energy used in the first stage is injected in the second stage to dry the last one. However, according to EP 0781 741 B1, in view of the dry conditions at the pre-evaporation outlet (40 to 60%), and the temperature conditions used in the dryer (120 C), the energy circuits do not are optimized.
    [0012] The present invention proposes to provide an energy solution for sludge drying by optimizing the method and regulating energy consumption, while adapting to the non-constant use of external energy at a low temperature (50 to 90 C).
    [0013] The objective of this invention is, in this way, to provide a method of drying paste-like products of the previously defined type, where energy consumption is minimized.
    [0014] The invention consists of controlling the pre-evaporation outlet dryness, or intermediate dryness, so that the heat that is recovered from the first evaporation stage is necessary and sufficient for drying in the second stage.
    [0015] According to the invention, a method of drying paste-like materials, in particular sludge from waste water treatment facilities, comprising two drying stages, namely: a first drying stage of an indirect type, supplied with hot fluid, which receives the sludge having a degree of dryness inlet Se, and releases the sludge having an intermediate degree of dryness Si and water vapor, which is channeled towards a condenser (8) in order to reheat a circuit for heating fluid, in particular water; a stage of formation of mud threads at the exit of the first stage; and the second drying stage of the mud wires heated directly by a gas, which is heated by the heating fluid circuit, this second stage distributing a product having a final dryness degree Sf, is characterized by the fact that the intermediate dryness degree If controlled according to the measured inlet dryness If and the desired outlet dryness Sf, for the minimum total energy consumption used for drying, the flow rate, pressure and / or temperature of the hot fluid supplying the first drying stage being adjusted accordingly.
    [0016] Preferably, the intermediate degree of dryness Si is determined for a minimum total energy consumption, based on the measurement of the degree of dryness input Se, the degree of dryness output Sf desired, and parameters comprising a specific coefficient c of the condenser, a specific coefficient β of the second drying stage, and if applicable additional free heat Qo. The intermediate degree of dryness Si can be controlled so that the heat recovered from the first stage through the condenser is necessary and sufficient for drying in the second stage.
    [0017] Advantageously, a heat circuit at a low temperature is used, which, in particular, is between 30 C and 90 C, to heat the second stage, comprising a liquid, in particular water, which is circulated according to a closed circuit and passes through the condenser in order to recover from there the heat from the condensed steam, and a liquid / gas heat exchanger in order to heat the gas of the second drying stage.
    [0018] The low temperature heat circuit may comprise an exchanger between the liquid in the circuit and a branch of thermal fluid from the first drying stage. The low temperature heat circuit can also comprise a heat exchanger in order to heat the liquid in the circuit by recovering cheap or dead low temperature energy.
    [0019] The invention also relates to an installation for the implementation of the previously defined method, comprising: a first dryer supplied with hot fluid, which receives the sludge having an Se dryness degree, and releases the sludge having a degree of intermediate dryness Si and water vapor, which is channeled towards a condenser in order to reheat a heating fluid for a second dryer; a device for forming mud strands at the outlet of the first dryer; and the second dryer to dry the pulp strands by means of a gas, in particular air, which is heated at least partially by the heat extracted from the condenser by means of the heating fluid, that second dryer releasing a product having a degree of final dryness Sf, an installation which is characterized by the fact that it comprises devices for controlling the intermediate dryness degree Si according to the measured dryness degree Se and the desired final dryness degree Sf, for a minimum total energy consumption used for drying, flow rate, pressure and / or temperature of the hot fluid supplying the first drying stage being adjusted accordingly.
    [0020] Preferably, the installation comprises a heat circuit at low temperatures, which, in particular, is between 30 C and 90 C, to heat the second stage, comprising a liquid, in particular water, which is circulated according to a closed circuit and passes through the condenser, in order to recover the condensed steam heat, and a liquid / gas heat exchanger in order to heat the gas of the second drying stage.
    [0021] Advantageously, the installation comprises an adjustable speed fan, the suction of which is connected to the steam and gas outlet of the first dryer, and the return flow which is connected to the condenser, the fan speed being controlled in order to to maintain a low pressure (of approximately few mbars) and controlled in the first dryer.
    [0022] The transfer of the paste between the outlet of the first dryer and the forming device (5) at the entrance of the second dryer can be guaranteed by a screw with a regulated speed core that allows gas impermeability at the outlet of the first dryer.
    [0023] The low temperature circuit for circulating the liquid of the installation may comprise: a part with a low temperature between 30 and 80 C, and preferably between 60 and 70 C, upstream of the condenser; a part with an intermediate temperature of between 40 and 90 C, and preferably between 70 and 80 C, at the outlet of the condenser; a heat exchanger between the liquid in the circuit and a free energy source, downstream or upstream of the condenser, to preheat the liquid in the circuit by a low temperature, low cost or free energy source, in particular the motor a joint generation unit, a heat pump, a wood or biogas heater, solar thermal systems, or another source of dead energy; at the outlet of the heat exchanger between the liquid in the circuit and the free energy source, a heat exchanger with a branch of thermal fluid that makes it possible to finish the reheating of the liquid in the circuit at a regulated temperature, for the second dryer, which is between 40 and 90 C, and preferably between 80 and 90 C; a heat exchanger between liquid and gas, and in particular water and air, which allows the liquid in the circuit to heat the gas of the second dryer, which is set in motion in particular by a circulation fan; a pump for circulating water in the circuit.
    [0024] Advantageously, the installation comprises regulation comprising a first regulation circuit in order to guarantee direct regulation of the intermediate dryness degree Si at the outlet of the first dryer, with a device for calculation and control, and, in particular, an element automation system that establishes an intermediate Sic dryness setpoint based on operating parameters.
    [0025] The regulation can be designed to determine an intermediate dryness determination point Sic according to the formula: Sic = (β + a * 556) / [(β - 89 * a) / Sf + 645 * oc / Se + Qo)] where: If is the measured input dryness degree (%) Sf is the final predetermined degree of dryness (%) β is a specific coefficient of the second drying stage (6), in kWh / TEE a is a specific coefficient of the capacitor (8) (without dimensions) and Qo is the free heat that can be added in kWh / TMS.
    [0026] The automation element can control a valve to control the flow rate, pressure or temperature of the thermal fluid according to the degree of intermediate dryness measured, this control being carried out by regulating the pressure of the thermal fluid in the case of a steam thermal fluid, or by regulating the flow rate or temperature (by mixing with a cold return of the thermal fluid) in the case of a thermal fluid of the organic fluid type.
    [0027] The installation can comprise regulation that consists of a regulation circuit that controls the amount of heat Q3 supplied in the exchanger between the thermal fluid and the liquid in the low temperature circuit.
    [0028] The regulation circuit that controls the amount of heat Q3 supplied in the exchanger between the thermal fluid and the liquid in the low temperature circuit can constitute a second regulation circuit. The regulation of the installation can be guaranteed only on the basis of this second circuit, by deviation (or overtaking) of the first regulation circuit.
    [0029] The heat exchanger between the thermal fluid and the liquid in the low temperature circuit can have as a control setting point the temperature of the liquid in the circuit at the outlet of the exchanger, this temperature allowing efficient operation of the exchanger between the fluid thermal and gas of the second dryer, and allowing the energy requirement of the second dryer to be balanced.
    [0030] The installation may comprise a regulation circuit according to which the heat Q3 supplied to the exchanger is measured by measuring the temperature and flow rate at the inlet and outlet of the exchanger, and, if the heat Q3 is higher to a specific set point that is close to zero but is not null, in order to always have a regulation range, the regulation modifies the output signal of the first regulation circuit, so that the heat supplied to the first dryer is adapted.
    [0031] In order to be in ideal conditions for the exchanger and condenser, the regulation of the installation may comprise a third regulation circuit that uses the temperature of the water circuit at the exit of the exchanger as a setting point. The third control circuit is advantageously designed to use a set point temperature that is defined with respect to a set point that depends on the flow rate of the paste measured at the paste supply pump, and when the temperature at the exchanger outlet between the liquid in the low temperature circuit and the gas in the second dryer increases, the flow rate of the circuit circulation pump decreases to a range that is acceptable for the components.
    [0032] According to the invention, a low temperature heat circuit is used to heat the second stage. This circuit enables the recovery of cheap or dead low temperature energy for heating the second dryer. The degree of dryness at the output of the first stage will be adapted according to the energy recovered from that cheap or dead energy.
    [0033] Dryer technologies also often include the recirculation of the sludge in order to avoid going through the plastic phase of the sludge (dryness 45 to 65%) inside the dryer, or preparing the paste upstream so that it is compatible with drying technology.
    [0034] The invention does not use the recirculation of the sludge and, in this way, makes it possible to obtain a greater exploration capacity of the system.
    [0035] Thus, the advantages provided by the method that is the subject of the invention in comparison with the existing techniques include: Energy consumption that is lower than that of all existing technologies, from 400 to 600 kWh / TEE instead of 1000 or 700 - 800 kWh / TEE; Possibility of reducing this consumption even further by optimizing the energy circuit based on low or medium temperature, cheap or free dead energy available; Use with any type of paste, by adapting the spaghetti formation technology, that is, forming the same in wires, for the mud in question; No use of a method for recirculating the paste.
    [0036] In addition to the supplies described above, the invention consists of a number of other supplies which will be explained explicitly hereinafter with respect to the illustrative modalities described with reference to the drawings which are attached, but are in no way limiting, in those drawings : Figure 1 is a diagram of an installation that implements the method according to the invention; Figure 2 is a diagram of a complementary device for the installation; e Figure 3 is a diagram illustrating the variation in the ratio of heat recovered to the heat used in the first drying stage, expressed as a percentage and shown on the geometric axis Y according to the temperature in degrees Celsius of non-condensing elements, at the outlet of the first drying stage, which is illustrated on the geometric X axis.
    [0037] With reference to figure 1 of the drawings, it can be seen that an installation according to the invention comprises a supply of slurry slurry with a degree of dryness generally between 16 and 30% guaranteed by a pump 1. Sludge is allowed sealed in a first dryer 2 of an indirect type. This dryer can be, for example, of a thin layer type, or with discs or blades. However, the disc dryer will be preferred.
    [0038] This indirect dryer 2 is heated by a thermal fluid circuit 3, the inlet and outlet temperatures, the flow rate and the pressure from which they are controlled. In this process, the amount of energy Q1 supplied to dryer 2 is controlled. The thermal fluid 3 can, for example, be steam or an organic fluid, in particular oil, the temperature of which can be between 180 ° C and 210 ° C by means of a non-limiting example.
    [0039] The indirect dryer 2 is also equipped with devices (not shown) for measuring the pressure, which are distributed evenly, and devices (not shown) for measuring the weight of the dryer. The air tightness of this dryer is produced so that the air intake is minimal. Additionally, for further thermal optimization, this dryer can be properly insulated.
    [0040] At the exit of the indirect dryer 2, the sludge is transported by a screw 4 that is accommodated in a cylindrical tube, thus allowing the reduction of the entry of air in the dryer at the exit of this dryer. Screw 4 is in particular made up of a coreless screw. The screw temperature can be maintained by the water heating network.
    [0041] At the exit of the screw, the sludge passes into a device 5 for the formation of threads, which is also known as spaghetti product, and which, by passing the sludge into calibrated holes, allows the creation of a spaghetti mat or yarn on belts 6a, 6b of a belt dryer 6.
    [0042] The belt dryer 6 can have one or more stages, in order to optimize the specific consumption of that dryer.
    [0043] A fan 7 makes it possible to control the pressure in the dryer 2 in order to keep the pressure low controlled. This point is essential since at first the dryer 2 may not be subjected to excessive pressure in order to avoid any odor release, but, in addition, the dryer 2 may not be subjected to excessively low pressure in order to prevent any air entering the extraction circuit of fan 7, which could considerably modify the thermal balance of the assembly.
    [0044] The air impermeability of dryer 2 is thus controlled by the perfect impermeability to air not only at the entrance, but also on the dryer inspection flaps. The air impermeability of the dryer outlet is guaranteed at the same time by: Mud outlet at the bottom part 2a of the dryer, part of which is filled with the mud;
    [0045] Presence of the screw without regulated speed core 4 in this lower part. This screw 4 allows the amount of mud in the dryer to always be sufficient to guarantee impermeability to air. This screw is regulated by the weight of the dryer 2.
    [0046] Submission to low pressure of this screw 4 at the screw outlet, in the spaghetti product 5, by means of a dedicated fan 15.
    [0047] Finally, the impermeability to air is guaranteed by the controlled maintenance of the pressure in dryer 2 by means of fan 7. Fan 7, which is connected by a duct to the high end of dryer 2, sucks in air, steam of water and non-condensable elements in order to transport them through a duct to a condenser 8. The rate of air flow in the fan 7 is controlled without allowing the vacuum (created by the condensation of the water vapor outlet from from dryer 2 and conveyor to condenser 8) give rise to uncontrolled suction in the dryer.
    [0048] The vapors that are sucked in by fan 7 contain water vapor and an amount of non-condensable elements that depends on the quality of the mud and the impermeability to air, but which, in general, is less than 10% by weight, with a well-controlled air tightness. These non-condensable elements are obtained from the evaporation of part of the sludge components and a very low air intake.
    [0049] These vapors then pass through the water condenser 8 where water circulates from a low temperature thermal circuit B1, which forms the basis for energy recovery.
    [0050] The low temperature circuit B1 consists of the following parts: a part B1.1 with a low temperature between 30 and 80 C, and preferably between 60 and 70 C, upstream of the capacitor 8; a part B1.2 with an average temperature of between 40 and 90 C, and preferably between 70 and 80 C, at the outlet of the condenser 8; at the condenser outlet, the water can additionally be reheated in an exchanger 9 by a "free" low temperature energy source, such as the engine of a joint generation unit, a heat pump, a biogas or a wood heater, solar thermal systems, or any other source of cheap or dead energy. It should be noted that according to the temperature areas referred to for this free heating source, this source can be positioned upstream or downstream of the condenser 8; At the outlet of the heat exchanger 9, a heat exchanger 10 for the thermal fluid 3, which is carried by a branch of the fluid supply duct 3, makes it possible to finish reheating the circuit to a temperature that is regulated for the belt dryer 6, among 40 and 90 C, and preferably between 80 and 90 C; This heated water then enables heating by means of a water and air exchanger 11 the air from the low temperature dryer 6 which is set in motion by means of the circulation fan 12.
    [0051] A P2 pump, in particular at the outlet of exchanger 11, for the circulation of water in circuit B1.
    [0052] The suction of the fan 12 is connected via a duct to the internal volume of the dryer 6, and the return flow is connected via a duct to the inlet of the exchanger 11 for the gas to be heated. The outlet of the exchanger 11 for the reheated gas is connected to the internal volume of the dryer 6.
    [0053] A circulation fan 13, the suction of which is connected by a duct to the internal volume of the belt dryer 6, and the return flow from which it is connected by a duct to the entrance of a water condenser 14, allows the this condenser 14 eliminates the moisture that is contained in the dryer 6. The air leaving the condenser 14 returns via a duct to the belt dryer 6.
    [0054] Another source of "free" heat that is assimilated to Q0 can be constituted by a heat pump C1 in a part of the circulation fan circuit 13 (see figure 2). The heat pump C1 comprises a circuit for a specific fluid which, when it reaches the liquid state in an evaporator 16, is evaporated by absorbing the heat, then compressed in a compressor 18, returned to the liquid state in a condenser 17 providing heat, then expanded in a pressure reduction valve 19 before being returned to the evaporator 16. The hot, humid air that comes out of the dryer 6 passes through the heat exchanger that consists of the evaporator 16. The water vapor from the hot air is condensed by means of evaporator 16, which recovers condensation energy. The condensation water is discharged through a duct 16a. The cold air leaving the evaporator 16, released from the condensed water vapor, is then reheated in the condenser heat exchanger 17, and is injected back into the dryer. The energy that is injected back into the capacitor 17 is assimilated in Q0, and must therefore be taken into account in the global system for the operation of the installation. EXAMPLES OF OPERATION CASE WITHOUT FREE ENERGY
    [0055] This is the case in which no free energy, or dead heat, is supplied to exchanger 9. Qo is then equal to zero.
    [0056] A slurry pumped by pump 1 has the following characteristics: Degree of dryness of 20%, level of MV (MV = volatile substances): 60%, temperature 12 C, flow rate 6245 kg / h (kg / hour) .
    [0057] The energy to dry this sludge in the first dryer 2 to a dryness level of 36.5% requires 2495 kW of thermal fluid 3, and the vapor flow rate through fan 7 is 3195 kg / h, including 290 kg / h of non-condensable elements. The temperature of these vapors is 100 C.
    [0058] At the outlet of the condenser 8, the non-condensable elements and the vapors have a temperature of 80 C, the remaining amount of water vapor is 164 kg / h, and the exchanged energy is 1575 kW.
    [0059] On the water circuit side B1, at the entrance B.1.1 of the water circuit before condenser 8, the temperature is 72 C, at the outlet of condenser 8 the water circuit temperature is 86 C, and the flow rate is 96.8 tons / hour.
    [0060] It is considered that no heat is provided by the exchanger 9. The water in the circuit is then heated to 88.74 C in the exchanger 10. The energy consumption is 318kW.
    [0061] The heat that is supplied to the air circuit of the fan 12 makes it possible to reduce the water temperature in the circuit to 72 C, while supplying the air circuit with an energy of 1826 kW. This heat energy makes it possible to evaporate the water in the belt dryer 6 to a dryness level of 90% with a ratio of 872 kWh / TEE.
    [0062] The total energy consumed by the system is 2495 + 318 = 2813 kW for an amount of evaporated water of 4997 kg / h. The specific consumption is therefore 563 kWh / TEE. CASE WITH FREE ENERGY
    [0063] This is the case when free energy, or dead heat, is supplied to exchanger 9. Qo is then positive.
    [0064] Consider the case of free energy, for example, of a joint generation motor, which makes it possible to supply 1000 kW thermal by heating water in the thermal circuit to 80 C in exchanger 9.
    [0065] For the slurry pumped by pump 1 with the following characteristics: The degree of dryness is 20%, the MV level: 60%, temperature 12 C, the flow rate of 6245 kg / h, the energy required to dry the mud in the first stage or first dryer 2 to a dryness level of 33% is 2184 kW.
    [0066] The vapors sucked in by fan 7 represent 2650 kg / h, of which 241 kg / h are non-condensable elements.
    [0067] At the outlet of condenser 8, the vapors have a temperature of 78 C, and the energy supplied to the water circuit B1 is 1353 kW, which represents a temperature increase from 70 C to 78 C from 145.4 tons /hour.
    [0068] The heat exchanger 9 of the joint generation engine makes it possible to heat the water from 78 to 83.9 C. The heat exchanger 10 to the fluid 3 allows the water to be reheated from 83.9 C to 84.1 C with a consumption of 44 kW.
    [0069] The energy supplied to the air is 2329 kW, and allows the sludge to dry to a degree of 90% dryness with a specific consumption of 900 kWh / TEE.
    [0070] Consumption excluding free energy is then 2184 + 44 = 2228 kW for 4997 kg / h of evaporated water, that is, a specific consumption of 445 kWh / TEE. OTHER APPLICATIONS
    [0071] This method of low-temperature drying and corresponding installation can be applied to any type of paste-like product, the preparation of which will have made it possible to remove stones or an excessively large amount of fibers that can prevent the production of spaghetti-type yarns .
    [0072] Applicable biomass pulp products may be wood, food processing products or animal processing products. ADJUSTMENT
    [0073] Consideration is now provided for the regulation of the method and installation of thermal drying for sludge obtained in particular from waste water treatment facilities, in order to make it possible to obtain a very low thermal energy consumption.
    [0074] The regulation can be used for any method and installation of drying any system for paste that must be dried, and that can be placed in the form of spaghetti in a pre-dried form.
    [0075] In the first place, there is a definition from a theoretical point of view of relationships between the various components of the installation.
    [0076] With reference to figure 3, the reaction of the condenser 8 to a variation in the temperature of the water circuit B1 is considered, and therefore, its cooling capacity.
    [0077] Taking into account 1000 kg / h of steam coming out of the fan 7 and the fact that these vapors enter at 100 C and consist of 10% of non-condensable elements, the amount of energy that is recovered in the condenser 8, expressed as a percentage of heat used in dryer 2, according to the outlet temperature of the non-condensable elements, shown on the geometric axis X, is shown in figure 3.
    [0078] If the level of non-condensable elements in the vapors obtained from the fan 7 is controlled, which is one of the principles of the invention, the amount of energy depends very little on the outlet temperature level of the non-condensable elements, provided that this does not exceed 83 C; outlet at 83 C = 70%, outlet at 70 C = 74%; output at 30 C = 78%.
    [0079] Additionally, since a steam / water condenser is involved, the exchange coefficients are very good, and the temperature of the vapors will depend above tube on the water circuit inlet temperature of the low temperature circuit B1.
    [0080] In the envisaged temperature range, the output, expressed by an alpha coefficient, can be considered to be 72% (alpha = 72% = 0.72) and be quite constant, even with a low variation in the outlet temperature non-condensable elements.
    [0081] The following part describes the mathematical bases of regulation according to the present invention.
    [0082] The following is applied: If: the degree of dryness of the inlet of mud at 1 51: the degree of intermediate dryness at the outlet of the dryer 2 and at the entrance of the screw 4 Sf: the degree of final dryness at the outlet of the dryer of the belt 6. 1. ton (1000 kg) of dry substance is taken into account at the pump inlet 1. The amount of water that evaporates in the first stage 2 is: (1 / Se-1 / Si).
    [0083] The amount of heat Q1 that is required for this evaporation is: slightly dependent on the composition of the sludge. [MS (dry substances), MV (volatile substances)] moderately dependent on the degree of dryness of the Se inlet and the inlet temperature of the mud; and highly dependent on the amount of water to be evaporated, and therefore on the factor: (1 / Se-1 / Si).
    [0084] In fact, in addition to evaporation, the heating of the mud must be carried out.
    [0085] This amount of heat Q1 can be expressed with relative precision using the theoretical formula: Q1 (Se, Si) = k (1 / Se-1 / Si) (1 +0.16 [Si (1-Se) Z (Si-Se)] Q1 in kWh Se and Si in% k being a constant equal to 556 with the units above.
    [0086] In the theoretical formula the dependence on the mud composition was eliminated, since it is only within the second order; this is the reason why this formula is validated with precision to approximately 5%.
    [0087] The heat that is required for the second drying 6 is approximately as: Q2 (SF, Si) = β * (1 / Si-1 / Sf) Q2 in kWh Si and Se in% β in kWh / TEE
    [0088] The parameter β corresponds to the specific heat of water evaporation in the second dryer 6, in kWh / TEE, depending on the selected belt drying technology, and in which the thermal losses of the heating circuit have been integrated. Since the mud is hot when it enters the belt dryer stage 6, β has an order of magnitude of [600-900] kWh / TEE.
    [0089] The heat that can be recovered from condenser 8 is defined as
    [0090] Q1, where a = approximately 0.72 as previously described.
    [0091] The free heat that is supplied to exchanger 9 is equal to Q0.
    [0092] The heat to be supplied by the thermal fluid 3 for the belt dryer 6 is equal to: Q3 = Max (Q2-ccQ1-Q0; 0).
    [0093] Q3 is the heat supplied by the thermal fluid 3 through the exchanger 10.
    [0094] The total heat supplied is equal to Qg = Q1 + Q3 = Q1 + Q2 - ocQ1 - Q0, provided that Q2 - ocQ1 - Q0> 0 and then Q1, when Q2 - ocQ1 - Q0 <0 This provides: Qg ( Si) = 556 (1-a) * (1 / Se-1 / Si) (1 + 0.16 [Si (1-Se) / (Si-Se)] * 1.03 + 850 ((1 / Si) - 1 / Sf) -Q0 as long as Q2-ccQ1-Q0> 0 and Qg (Si) = 556 (1 / Se-1 / Si) (1 + 0.16 [Si (1-Se) / (Si-Se) )] subsequently.
    [0095] The objective is to minimize this Si function. This function is a decreasing Si function, since Q2-ccQ1-Q0> 0, then an increasing Si function.
    [0096] The minimum of this function is obtained when all the heat from the first drying stage 2 is necessary and sufficient to heat the second stage 6. Thus, when Q2 = aQ1 + Q0.
    [0097] This function is solved according to equation [A] below. [A] Si = [β + α * 556) / [(β-89 * α) / Sf + 645 * α / Se + Q0). Thus, it is known that: β that depends on the technology used for 6 α belt dryer that is very stable according to the outlet temperature of the non-condensable elements Sf which is fixed QO which is fixed and is reduced to the amount of energy which can be supplied for 1 ton of DM (dry substances), it is possible to determine the ideal degree of dryness Si as a function of Se. Numerical application: β = 850 oc = 0.72 Sf = 90% Qo = 0 If = 20% Si = 39.1%
    [0098] According to the invention, the minimization of the heat consumed within the context of drying in two stages is obtained by recovering the high temperature energy from the first stage 2 by condensing the steam in order to heat a low thermal circuit temperature B1 (40 to 90 C), which makes it possible to heat the second drying stage 6. The present invention also makes it possible to take into account the regulation of the installation of an exchanger 9 to recover the dead heat from another installation (heat Q0) .
    [0099] According to the invention, the intermediate dryness Si is controlled according to the measured inlet dryness Se and the desired outgoing dryness Sf.
    [0100] The principle of installation and method regulation is, therefore, based on the measurement of the degree of dryness Se and regulation parameters Sf, β, a and Qo, to establish a setpoint of degree of dryness output Si The measurement of the intermediate dryness degree Si is guaranteed by a dryness sensor 20 at the outlet of dryer 2.
    [0101] Other adjustments complete and guarantee the first adjustment, which is guaranteed by a first adjustment circuit.
    [0102] The installation comprises a plurality of regulation circuits:
    [0103] The purpose of the first regulation circuit is to direct the regulation of the intermediate dryness Si at the outlet of the dryer 2. A calculation and control device, and in particular an automation element M, is provided in order to establish an intermediate dryness set point Sic, in particular based on the formula [A] previously provided, and the values of the parameters and quantities supplied by the different measurement sensors.
    [0104] The automation element M controls a control valve 21 for the flow rate, pressure or temperature of the thermal fluid, according to the intermediate dryness Si measured by sensor 20. This control can be carried out by regulating the flow rate of the thermal fluid, in the case of a thermal steam fluid, or by regulating the flow rate or temperature (by mixing with cold return of the thermal fluid), in the case of a thermal fluid of the type of organic fluid.
    [0105] Since the reaction times of the installation are long, controls can be carried out according to these reaction times.
    [0106] A second regulation circuit controls the amount of heat Q3 supplied in the exchanger 10 by the thermal fluid 3 for the water of the low temperature circuit B1. In fact, it was previously mentioned that the ideal energy is obtained when this amount of heat Q3 is equal to 0, without being nematic.
    [0107] The purpose of this exchanger 10 is to control the temperature of the water circuit at the outlet of the exchanger 10, measured by a sensor 22 that transmits the data to the automation element M. This temperature allows the efficient operation of the exchanger 11, and allows that the energy requirement of the low temperature dryer 6 is well balanced.
    [0108] If the temperature at the outlet of the exchanger 10 is not reached, it is because the heat that is removed from the exchanger 11 is greater than that supplied by the condenser 8, and therefore the ideal energy is no longer obtained.
    [0109] The heat Q3 supplied to the exchanger 10 is therefore measured by measuring the temperature and flow rate at the inlet of the exchanger 10 by a set of sensors 23e, and at the outlet of the exchanger 10 by a set of sensors 23s, the sensors being connected to the automation element M in order to transmit the measured values.
    [0110] If the heat Q3 is greater than a specific setpoint that is close to 0 but is not null, in order to always have a regulation range, the second regulation circuit modifies the output of the first regulation circuit previously described, so that the heat supplied to the first dryer 2 is adapted.
    [0111] It is also possible to adjust the installation and the system only by means of the second regulation circuit through the deviation (overtaking) of the first regulation circuit.
    [0112] Finally, in order to be in ideal conditions for the exchanger 11 and the condenser 8, a third control circuit uses the temperature of the water circuit at the outlet of the exchanger 11 as a setting point, measured by a sensor 24 which is connected to the automation element in order to transmit the temperature value. This temperature is defined in relation to a set point that depends on the flow rate of the sludge measured at pump 1.
    [0113] If the temperature at the outlet of exchanger 11 increases, the flow rate of the circulation pump P2 in the circuit decreases to a range that is acceptable for the equipment.
    [0114] This triple circuit is self-stable. In fact, if the need for heat in the belt dryer 6 decreases, the temperature at the outlet of exchanger 11 will increase, and the flow rate of the circulation pump will decrease in exchanges 11 and 8. In condenser 8, the temperature difference ΔT between the outlet and inlet of condenser 8 for water in circuit B1 will increase, and the temperature at the inlet of exchanger 10 will increase, which will reduce the amount of heat that needs to be supplied to exchanger 10 by thermal fluid 3, below the value of configuration point ,.
    [0115] In this case, the automation element M will send an order to the valve 21 of the dryer 2 to decrease the flow rate of the thermal fluid 3 in the dryer 2, which will reduce the degree of intermediate dryness Si and increase the need for evaporation on the belt conveyor, which will rebalance the temperature at the outlet of the exchanger 11.
    [0116] Additionally, a temperature setpoint at the exchanger outlet 11 will be defined in relation to the flow rate of the pump 1 which is supplied to the automation element M by a sensor 25.
    [0117] In fact, if the flow rate of pump 1 decreases, with the degree of intermediate dryness Si being regulated by the first regulation circuit, the absolute amount of heat in the second dryer 6 decreases. The exchange in the exchanger 11 will therefore also be decreased, and if the inlet temperature is fixed, the outlet temperature will increase. It is therefore necessary to lower the flow rate set point so that cooling is increased.
    [0118] It will be appreciated that the present invention is not limited to the illustrative modalities described and / or represented, but incorporates all variations that are within the scope of the appended claims.
    权利要求:
    Claims (20)
    [0001]
    1. Method of drying paste-like materials, in particular sludge from waste water treatment facilities, comprising two drying stages, namely: a first drying stage (2) of an indirect type, supplied with hot fluid, which receives the sludge having an inlet dryness degree Se, and sends the sludge having an intermediate dryness degree Si and water vapor, which is channeled towards a condenser (8) in order to reheat a circuit for the fluid heating, in particular water; a step (5) of formation of mud threads at the exit of the first stage; and the second stage (6) of drying the wires of the mud heated directly by a gas, which is heated by the heating fluid circuit, this second stage 96) sending a product having a final dryness degree Sf, characterized by the fact that the intermediate dryness degree Si controlled according to the measured inlet dryness If and the desired dryness degree Sf, for a minimum total energy consumption used for drying, the flow rate, pressure and / or temperature of the hot fluid (3) supplying the first drying stage (2) being adjusted accordingly.
    [0002]
    2. Method according to claim 1, characterized in that the intermediate degree of dryness Si is determined for a minimum total energy consumption, based on the measurement of the degree of dryness inlet Se, the degree of dryness inlet Sf desired, and parameters comprising a specific coefficient α of the condenser (8), a specific coefficient β of the second drying stage (6), and if applicable the additional free heat Qo.
    [0003]
    3. Method according to claim 1 or 2, characterized in that the degree of intermediate dryness Si is controlled so that the heat recovered from the first stage by means of the condenser (8) is necessary and sufficient for drying in the second stage (6).
    [0004]
    4. Method according to any one of the preceding claims, characterized by the fact that a heat circuit (B1) at a low temperature is used, which, in particular, is between 30 and 90 C, to heat the second stage (6) , comprising a liquid, in particular water, which is circulated according to a closed circuit and passes through the condenser (8) in order to recover from there the heat from the condensed steam, and a liquid / gas heat exchanger ( 11) in order to heat the gas of the second drying stage (6).
    [0005]
    5. Method according to claim 4, characterized in that the low temperature heat circuit (b1) comprises an exchanger (10) between the liquid in the circuit (B1) and a branch of thermal fluid (3) of the first stage drying (2).
    [0006]
    6. Method according to claim 4 or 5, characterized in that the low temperature heat circuit (B1) comprises a heat exchanger (9) in order to heat the liquid in the circuit by recovering cheap low temperature energy or free.
    [0007]
    7. Installation for the implementation of a method, as defined in any one of the previous claims, characterized by the fact that it comprises: a first dryer (2) supplied with hot fluid, which receives the sludge having an inlet dryness degree, and sends the sludge having an intermediate degree of dryness Si, and water vapor, which is channeled towards a condenser (8) in order to reheat a heating fluid for a second dryer (6); a device (5) for forming mud strands at the outlet of the first dryer (2) and the second dryer (6) for drying the mud strands by means of a gas, in particular air, which is heated at least partially by heat extracted from the condenser (8) by means of the heating fluid, this second dryer (6) sending a product having a final degree of dryness Sf, characterized by the fact that it comprises means (M, 21) for controlling the intermediate degree of dryness Si according to the measured inlet dryness degree If and the desired outward dryness degree Sf, for a minimum total energy consumption used for drying, the flow rate, pressure and / or temperature of the hot fluid (3) supplying the first drying stage (2) being adjusted accordingly.
    [0008]
    8. Installation, according to claim 7, characterized by the fact that it comprises a heat circuit (B1) at a low temperature, which, in particular, is between 30 and 90 C, to heat the second stage (6), comprising a liquid, in particular water, which is circulated according to a closed circuit and passes through the condenser (8), in order to recover the condensed steam heat, and a liquid / gas heat exchanger (11) in order to heat the gas from the second drying stage (6).
    [0009]
    9. Installation, according to claim 7 or 8, characterized by the fact that it comprises an adjustable speed fan (7), the suction of which is connected to the steam and gas outlet of the first dryer (2), and the return flow from which it is connected to the condenser (8), the fan speed being controlled in order to keep the low pressure low (in the order of a few mbars) and controlled in the first dryer (2).
    [0010]
    10. Installation according to any of claims 7 to 9, characterized by the fact that the transfer of sludge between the outlet of the first dryer (2) and the forming device (5) at the entrance of the second dryer (6) is guaranteed by a screw with a regulated speed core (4) that allows gas impermeability at the outlet of the first dryer (2).
    [0011]
    11. Installation according to claim 8, characterized by the fact that the low temperature circuit (B1) for liquid circulation comprises: a part (B1.1) with a low temperature of between 30 and 80 C, and preferably between 60 and 70 C, upstream of the capacitor (8); a part (B1.2) with a median temperature of between 40 and 90 C, and preferably between 70 and 80 C, at the outlet of the condenser (8); a heat exchanger (9) between the liquid in the circuit (B1) and a free energy source, downstream or upstream of the condenser (8), to reheat the liquid in the circuit (B1) by a low temperature energy source , low cost or free, in particular the engine of a joint generation unit, a heat pump, a wood or biogas heater, solar thermal systems, or other source of dead energy; at the outlet of the heat exchanger (9) between the liquid in the circuit (B1) and the free energy source, a heat exchanger (10) with a branch of thermal fluid (3) that makes it possible to finish the reheating of the liquid in the circuit (B1 ) at a regulated temperature, for the second dryer (6), which is between 40 and 90 C, and preferably between 80 and 90 C; a heat exchanger (11) between liquid and gas, and in particular water and air, which allows the liquid in the circuit (B1) to heat the gas of the second dryer (6), which is set in motion in particular by a fan circulation (12); a pump (P2) for circulating water in the circuit (B1).
    [0012]
    12. Installation, according to any of claims 7 to 11, characterized by the fact that it comprises regulation comprising a first regulation circuit in order to guarantee direct regulation of the intermediate dryness degree Si at the outlet of the first dryer (2), with a device for calculation and control, and in particular an automation element (M) that establishes a set point of intermediate degree of dryness Sic based on the operational parameters.
    [0013]
    13. Installation, according to claim 12, characterized by the fact that the regulation is designed to determine an intermediate dryness set point Sic (%) according to the formula: Sic = (β + α * 556) / [ (β-89 * α) / Sf + 645 * α / Se + Qo)] where: If it is the measured degree of input dryness (%) Sf is the final predetermined degree of dryness (%) β is a specific coefficient of second drying stage (6), in kWh / TEE a is a specific coefficient of the condenser (8) and Qo is the free heat that can be added in kWh / TMS.
    [0014]
    14. Installation according to claim 12 or 13, characterized in that the automation element (M) controls a valve (21) to control the flow rate, pressure or temperature of the thermal fluid (3) according to measured intermediate dryness degree, this control being carried out by regulating the pressure of the thermal fluid in the case of a thermal fluid of steam, or by regulating the flow rate or temperature (by mixing with a cold return of the thermal fluid) in the case of a thermal fluid of an organic fluid type.
    [0015]
    15. Installation according to any of claims 7 to 11, characterized by the fact that it comprises regulation consisting of a regulation circuit that controls the amount of heat (Q3) supplied in the exchanger (10) between the thermal fluid and the liquid in the low temperature circuit (B1).
    [0016]
    16. Installation, according to the combination of the claim and any one of claims 12 to 14, characterized by the fact that the regulation circuit that controls the amount of heat supplied in the exchanger (10) between the thermal fluid and the liquid in the circuit low temperature (B1) constitute a second regulation circuit, the regulation of the installation being able to be guaranteed only based on this second circuit, by the deviation (or overtaking) of the first regulation circuit.
    [0017]
    17. Installation according to claim 15 or 16, characterized by the fact that the heat exchanger (10) between the thermal fluid and the liquid in the low temperature circuit (B1) has the temperature of the temperature as a control setting point liquid in the circuit (B1) at the outlet of the exchanger (10), this temperature allowing the efficient operation of the exchanger (11) between the thermal fluid and the gas of the second dryer (6), and enabling the energy requirements of the second dryer ( 6) be balanced.
    [0018]
    18. Installation according to any of claims 12 to 17, characterized in that it comprises a regulation circuit according to which the heat (Q3) supplied to the exchanger (10) is measured by measuring the temperature and flow rate at the inlet and outlet of the exchanger (10), and, if the heat (Q3) is greater than a specific setpoint that is close to zero, but not null, in order to always have a range of regulation, regulation modifies the output signal of the first regulation circuit, so that the heat supplied to the first dryer (2) is adapted.
    [0019]
    19. Installation according to any one of claims 12 to 18, characterized in that, in order to be in ideal conditions for the exchanger (11) and the condenser (8), the regulation comprises a third regulation circuit that it uses the temperature of the water circuit at the exchanger outlet (11) as the setting point.
    [0020]
    20. Installation according to claim 19, characterized in that the third regulation circuit is designed to use a setpoint temperature that is defined in relation to a setpoint that depends on the flow rate of the slurry measured in sludge supply pump (1), and when the temperature at the exchanger outlet (11) between the liquid in the low temperature circuit (B1) and the gas in the second dryer (6) increases, the flow rate of the circulation pump (P2) of the circuit (B1) decreases to a range that is acceptable for the components
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    同族专利:
    公开号 | 公开日
    RU2012126090A|2013-12-27|
    BR112012012380A2|2018-04-17|
    CA2781038C|2017-07-04|
    JP2013511693A|2013-04-04|
    DK2504649T3|2015-01-05|
    AU2010320518A1|2012-06-07|
    JP5847726B2|2016-01-27|
    FR2953005A1|2011-05-27|
    EP2504649A1|2012-10-03|
    RU2555047C2|2015-07-10|
    ES2477226T3|2014-07-16|
    EP2504649B1|2014-04-02|
    MX2012005877A|2012-06-19|
    US8832962B2|2014-09-16|
    BR112012012380B8|2020-12-22|
    CN102713481A|2012-10-03|
    CN102713481B|2014-09-17|
    PT2504649E|2014-07-10|
    NZ600116A|2013-05-31|
    KR101878644B1|2018-07-16|
    FR2953005B1|2011-12-09|
    PL2504649T3|2014-10-31|
    CA2781038A1|2011-05-26|
    KR20120089753A|2012-08-13|
    AU2010320518B2|2016-04-28|
    US20120304488A1|2012-12-06|
    BR112012012380A8|2020-05-12|
    WO2011061715A1|2011-05-26|
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    法律状态:
    2019-01-08| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2019-10-08| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2020-06-09| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2020-09-15| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 19/11/2010, OBSERVADAS AS CONDICOES LEGAIS. |
    2020-12-22| B16C| Correction of notification of the grant [chapter 16.3 patent gazette]|Free format text: REF. RPI 2593 DE 15/09/2020 QUANTO A PRIORIDADE UNIONISTA. |
    优先权:
    申请号 | 申请日 | 专利标题
    FR0905607|2009-11-23|
    FR0905607A|FR2953005B1|2009-11-23|2009-11-23|PROCESS AND INSTALLATION FOR DRYING PASTE MATERIALS, IN PARTICULAR SLUDGE OF PURIFICATION STATIONS|
    PCT/IB2010/055304|WO2011061715A1|2009-11-23|2010-11-19|Method and facility for drying slurry-like materials, in particular sludge from wastewater treatment plants|
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