• 专利附录
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    • 专利摘要:
    Procedure for the thermal hydrolysis of organic matter in stationary regime, with double explosion of steam and with total energy recovery, which consists, as a minimum, of the stages of 1) feeding, stepped pressurization and sequential injection of vapors of low pressure levels, medium and high; 2) first stage of hydrolysis by consecutive operations of steam explosion with steam production of medium pressure level and thermal reaction; 3) second stage of hydrolysis consisting of steam explosion and production of low pressure steam. An installation for the implementation of the process, comprising pumps for stepped pressurization, fluid-steam mixers, valves, mixers, decompression elements, tanks, piping and instrumentation and control systems. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2608598A1
    申请号:ES201631577
    申请日:2016-12-13
    公开日:2017-04-12
    发明作者:Rafael GONZÁLEZ CALVO；Diego FERNÁNDEZ-POLANCO
    申请人:Te Consulting House 4 Plus Sl；
    IPC主号:
    专利说明:

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    DESCRIPTION
    Procedure and installation for the thermal hydrolysis of organic matter in stationary regime and with total energy recovery
    Technical sector of the invention
    The invention, which includes a procedure and installation for its implementation, applies to the field of organic matter treatment, including sewage sludge, domestic and industrial waste and any other matter. Find special application as a treatment prior to anaerobic digestion of solids.
    Background of the invention
    In different industrial processes it is necessary to modify the physical and chemical structure of solids, for which a pre-treatment is used. In the particular case of anaerobic digestion of solids, the hydrolysis stage (solubilization, liquefaction) limits the overall kinetics of the process. To improve the kinetics of the hydrolysis stage, different physical, chemical and biological processes are applied as a pre-treatment to anaerobic digestion, with the consequent improvement of the global methanization process. The thermal hydrolysis process is based on subjecting the solid to high temperatures and pressures for relatively long periods of time, usually greater than 30 minutes. Subsequently, taking advantage of the high pressure, the hot dough can undergo a sudden decompression process or flash process, in order to achieve the so-called vapor explosion effect that generates breakage of the structure of the solids. Other processes use heat exchangers to recover energy from the hot dough.
    All technologies that recover energy by recirculating and condensing the steam produced in the flash stage to heat the feed that reaches the hydrolysis stage, use steam of a single pressure level. As this pressure corresponds to that of the flash camera, the steam produced is low pressure. With this configuration it is not possible to take advantage of all the energy contained in the steam, which leads to energy-efficient systems. To reduce energy consumption, the power is concentrated, to very high values, with the consequent increase in costs attributable to this operation, which requires the use of high amounts of chemical products. The patent ES2570812A1, aims to solve the inefficiency by raising the pressure of the steam that comes out of the flash chamber using a mechanical compressor that uses electrical energy and is of complex maintenance, for compressing steam that contains aggressive condensables and incondensables; In addition to using electrical energy, the system is energetically inefficient.
    The ES2538176B1 patent resolves said energy inefficiency with a radically different conceptual design, which differentiates it from all existing processes and facilities. Instead of using steam of a single pressure level, use steam with two pressure levels.
    With this configuration and in accordance with the laws of thermodynamics, it is possible to fully recover the energy content of the vapors, making the facilities energy efficient even while operating with moderate concentrations of solids.
    Based on this fact, all procedures and installations operating with steam explosion use a thermal reaction stage sequence followed by steam explosion. The claimed process uses a sequence of steam explosion stages + thermal reaction stage + steam explosion stage. This procedure improves the overall kinetics of the process, which leads to more compact installations and with lower installation, operation and maintenance costs.
    The present patent derives and is continuation of the ES2538176B1 patent, expanding its field of actuation. The evolution of the pumping equipment and the appearance of new materials allow, at present, to use mechanical systems to drive the fluid to be hydrolyzed reliable, low maintenance and capable of withstanding the operating conditions. Faced with this new situation, this patent, maintaining the
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    fundamental characteristic of operating with total energy recovery, with low residence times and with sequence of stages steam explosion + thermal reaction + steam explosion, introduces the possibility of using mechanical pumping systems.
    Explanation of the invention
    The present process for the continuous thermal hydrolysis of organic matter consists, as a minimum, of the stages: 1) feed, step pressurization and sequential injection of vapors of low, medium and high pressure levels; 2) first stage of hydrolysis through consecutive operations of steam explosion with steam production of medium pressure level and thermal reaction; 3) second stage of hydrolysis consisting of steam explosion and low pressure steam production.
    In the usual practice of sludge generating plants, the temperature at the entrance to the process is that of the environment, however, there is a tendency to take advantage of the energy from surplus currents. This implies a possible wide range of inlet temperatures than for stage 1, which requires a flexible conceptual design of the procedure and facilities.
    In stage 1, the organic matter to be hydrolyzed (5) is pressurized and heated until it reaches the setpoint values prior to its entry (11) to stage 2. Pressurization is achieved by at least the mechanical impulse equipment of the fluid (20) and (21). Heating is achieved by injecting at least low (13), medium (15) and high (16) pressure vapors. To achieve an adequate quality of the fluid-vapor mixture, at least mixers (17), (18) (19) are used.
    Mechanical fluid impulse equipment (20) and (21) and any other that is decided to be installed, are selected from any type of pump capable of driving fluids, including non-Newtonian ones, and high viscosity suspensions. Particularly in a variant of the invention and thanks to the staggering of pressures centrifugal pumps can be used, cheaper and with lower maintenance costs than positive displacement pumps used by other technologies. They must supply pressures between 1 and 10 barg and operate in the temperature range 20 - 180 ° C.
    The mixers (17), (18), (19), are selected from both static and dynamic equipment.
    Taking into account the great variability of possible types of organic matter and the conditions of pressure, temperature and concentration of the feed (5), the procedure and installation must be flexible. In a variant of the invention the output current (6) of the pump (20) is divided into the currents (7) and (9). The current (7) after passing through the mixer (17) is returned to the tank (2), so that the pump (20) acts simultaneously as a pressurization and recirculation system. In another variant, by closing the valve (14) all the current (6) from the pump outlet (20) is carried directly to the mixer (18), thus breaking the recirculation loop. The feed (5) and the low steam (13) are taken directly to the tank (2).
    In a variant of the invention, the mixer (17) is an ejector that uses the mass recirculated by the pump (20) as the driving fluid. In this way, in addition to achieving a good mixture, it is possible to reduce the pressure of the chamber (4) and the temperature of the outlet current (24). This fact leads to lower energy consumption in the process.
    According to the energy balances, the fluid (10) cannot reach temperatures greater than 170 ° C, which the literature marks as a limit for the development of secondary reactions that lead to the formation of recalcitrant, non-biodegradable and potentially toxic compounds. In the mixer (19) the extremely fast mixture of live steam (16) and fluid to be hydrolysed (10) is achieved, reaching temperatures that can reach 220 ° C. The heating is carried out in extremely short times, less than 5 seconds, so that secondary reactions cannot occur.
    The fluid (11) at high temperature and pressure passes through the element (22) capable of causing instantaneous decompression, with the consequent decrease in temperature, generating a first break in the structure of the
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    solid by steam explosion mechanism. In the tank (3), a medium pressure steam stream (15) is produced which leads to stage 1. The liquid fraction that has undergone a first steam explosion break is maintained inside the tank (3 ) a time between 1 and 15 minutes, thus allowing the hydrolysis reaction process to be carried out by temperature. The pre-hydrolyzed organic matter stream (12) is conducted to step 3.
    In a variant in which the sewage sludge is operated without domestic treatment, the tank (3) is controlled so that the temperature of the liquid contained inside it can never exceed 170 ° C. In another variant in which it is operated with previously digested sludge or with organic matter of another origin, the temperature can rise to higher values, always below the limit of occurrence of secondary reactions.
    The fluid (12) whose pressure is that of equilibrium with the temperature imposed as a setpoint to the tank (3), is depressurized when passing through the element (23). In the tank (4) the separation of a low pressure steam stream (13) takes place, which is carried to stage 1 and the stream of hydrolyzed organic matter (24) that is digested.
    In a variant of the invention the pressure of the tank (4) is slightly higher than atmospheric, in the range 0 - 0.2 barg. In another variant and by the effect of the mixer (17), which in this variant is an ejector that acts as a vacuum system, the pressure in the tank (4) can be maintained between -0.5 and 0 barg.
    As a consequence of the procedure used, the system not only operates continuously, but unlike existing technologies it also operates in a stationary regime. This means that once the operation variables (eg flow rates, levels, pressures and temperatures) are preset, they do not change over time. This behavior leads to processes that operate with greater stability, require simpler control systems, are more flexible and robust and obtain better yields.
    Brief description of the figures
    Figure 1 represents a diagram of the installation for the implementation of an installation according to the invention.
    Explanation of a form of realization
    Following the figure 1 the procedure according to the invention that is claimed and the means used for the realization of an installation is described.
    The means used are: tanks or tanks (2), (3), (4); mechanical equipment for impulsion and pressurization of the fluid (20), (21); steam-fluid mixers (17), (18), (19); expansion elements (22), (23).
    In the selected variant, sewage sludge sludge is hydrolyzed, previously concentrated and at room temperature (5). In the ejector (17) the feed mixture (5) is produced, with low pressure steam (13) and with the recirculation current (7). The ejector output current (8) is returned to the tank (2), in order to close a recirculation loop. All the low steam (13) condenses in the system. Depending on the design conditions and the recirculation flow rates that are imposed, the current (9) that leaves the recirculation loop has a temperature between 70 and 100 ° C and a pressure with values between 3 and 8 barg.
    The current (9) after the first stage of pressurization and heating receives in the mixer (18) the medium pressure steam (15). According to the energy balances, in operating conditions the temperature after the incorporation of medium and high pressure steam currents moves between 120 and 160 ° C, without reaching the thermal level corresponding to the development of secondary reactions. This fluid (10) is pressurized by the pump (21), reaching pressures between 8 and 20 barg. In the ultra-fast mixer (19) the fluid receives a live steam injection (16) with a pressure between 10 and 22 barg, capable of raising its temperature to 160-220 ° C.
    After this ultra-rapid heating, the high temperature and pressure sludge (11) passes through the decompression element (22) and is cleaved in the tank (3) in a medium pressure vapor stream (15) which is conducted to the stage 1 and in a liquid stream (12). The liquid is kept in the tank (3), for a preset time, which varies between 1 and 15 minutes. With this sequence the organic matter is first subjected to a steam explosion process and then to a reaction process by thermal process. Consequently the tank (3), fulfills the double function of flash tank and reactor. In the case described, the temperature inside the tank (3) is maintained at a preset and controlled setpoint value in the range 140 and 180 ° C.
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    After remaining in the tank (3) during the predetermined reaction time, the stream (12) of pre-hydrolyzed organic matter, with pressure between 3 and 9 barg, passes through the decompression element
    (23) and in the tank (4), which acts as a flash camera is cleaved in a stream of low pressure steam (13) that is carried to stage 1 and in a stream (24) of hydrolyzed sludge that is carried to digestion. The pressure
    15 of the tank (4) can vary between - 0.5 and + 0.5 barg. In the variant described and with the liquid ratio that recirculates the pump (20) the pressure in the tank (4) is -0.1 barg and the current outlet temperature
    (24) is 97 ° C.
    权利要求:
    Claims (6)
    [1]
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    1. Procedure for the continuous thermal hydrolysis of any type of organic matter that, to fully recover the energy and optimize the hydrolysis kinetics, comprises as a minimum stages of 1) feeding, stepped pressurization and sequential injection of pressure level vapors low, medium and high; 2) first stage of hydrolysis through consecutive operations of steam explosion with steam production of medium pressure level and thermal reaction; 3) second stage of hydrolysis consisting of steam explosion and low pressure steam production.
    [2]
    2. Procedure which according to claim 1 and differently from the currently existing procedures is characterized by a stage of sequential feeding, pressurization and injection of the heating vapors, characterized by:
    - use a stepped pressure increase system, which allows receiving and using steam from different pressure levels. In any circumstance the vapors from the tanks (3) and (4) are injected into the system. In accordance with the laws of thermodynamics, this procedure allows a total recovery of energy, without the need to operate with very high concentrations of organic matter.
    - use systems with at least two pumps, which when pressurized in a staggered manner allow adequate injection of the vapors into the corresponding liquid-gas mixers.
    - Due to the pressure scaling, use centrifugal pumps instead of positive displacement pumps, which are more expensive and difficult to maintain.
    - reach temperatures and pressures of the feed to the hydrolysis stage (11) of up to 22 barg and 220 ° C, higher than the conventional ones.
    - use low pressure steam mixing systems that allow lowering the pressure of the chamber of the second flash (4) to values between 0 and -0.5 barg, with the consequent decrease in the outlet temperature of the hydrolyzed organic matter and its impact on net energy consumption.
    - use ultra-fast live steam mixing systems, so that the mixture to be hydrolyzed is only at a temperature higher than the critical appearance of secondary reactions for times less than 5 seconds. In those short times the extent of side reactions is negligible.
    [3]
    3. Procedure that according to claim 1 and differently from those currently existing consists of a first stage of hydrolysis, characterized by:
    - use a sequence of steam explosion + thermal reaction stages, which improves the overall kinetics of the process by reducing the size of the facilities.
    - use a tank (3) that simultaneously operates as a flash tank, facilitating a first rupture of the physical structure of organic matter, and as a reactor that facilitates the hydrolysis reaction by temperature.
    - apply the hydrolysis reaction by temperature to sludge that has previously undergone a steam explosion process, with which the reaction kinetics is markedly increased, allowing operation with temperatures between 140 and 180 ° C and reaction times lower than 15 minutes.
    [4]
    4. Procedure that according to claim 1 and differently from those currently existing consists of a second stage of hydrolysis, characterized by:
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    - make a second steam explosion from pressures between 3 and 10 barg to pressures between -0.5 and 0.5 barg.
    - producing a low pressure steam that is conducted to step 1 of claim 1.
    [5]
    5. Procedure that according to the preceding claims and differently from those currently existing operates not only continuously but also in a stationary regime with the consequent stability of the process and ease of control, which gives the procedure great operational robustness.
    [6]
    6. An installation (1) for continuous thermal hydrolysis of organic matter, which according to claims 1, 2, 3, 4 and 5 can treat any type of solids and is especially suitable for treating sludges produced in water treatment plants residual and that achieves energy self-sufficiency by operating with dry matter concentrations lower than those required by existing technologies. The installation includes:
    - at least two pumps (20) and (21) for the stepped pressurization of the organic matter fed. In the first phase, the pressure of the current (9) rises to values between 3 and 8 barg. In the second phase, the pressure of the current (11) is raised to values between 10 and 22 barg.
    - at least three static or dynamic fluid-vapor mixers (17), (18), (19), which allow a stepped increase in temperature taking advantage of at least the low (13) and medium pressure (15) vapors produced in the flash stages
    - valve (14) that can act as a pressure control or shut-off valve.
    - mixer (17), which depending on the characteristics of the feed (5) can be an ejector, which reduces the pressure of the tank (4) to values between 0 and -0.5 barg.
    - a mixer (19) that receives live steam and that to prevent the occurrence of secondary reactions operates with mixing times of less than 5 seconds.
    - a current (11) whose values of pressure (up to 22 barg) and temperature (220 ° C), far exceed the limits imposed by other technologies.
    - decompression elements that can be selected from narrowings, nozzles or valves (22) and (23) that are sized according to the flow to be treated, to produce the pressure drop generated by the steam explosion mechanism. In the device (22) the inlet pressures can vary between 10 and 22 barg, with a maximum outlet pressure of 8 barg. For the device (23) for a maximum inlet pressure of 8 barg, the outlet pressure moves in the range -0.5 - 0.5 barg.
    - tanks (3) and (4) that operate as flash chambers in which medium pressure steam (15) and low pressure (13) are produced, which when condensed are used to increase the temperature of the organic matter to be hydrolyzed. Also the tank (3) acts as a reactor. The operating temperatures in the tank (3) can be set between 140 and 180 ° C, while in the tank (4) they are set between 80 and 110 ° C.
    - instrumentation and control systems, not indicated in figure 1, so that according to claim 5, which involves stationary regime, allow to preset and keep constant the desired value of any of the operation variables at all points of the installation.
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    WO2015032552A1|2013-09-06|2015-03-12|Veolia Water Solutions & Technologies Support|Method and device for continuous thermal hydrolysis with recovered steam recirculation|
    WO2015189449A1|2014-06-11|2015-12-17|Te Consulting House 4 Plus, Sl|Method and facility for thermal hydrolysis of organic matter having short residence times and no pumps|
    WO2016079361A1|2014-11-19|2016-05-26|Aquatec, Proyectos Para El Sector Del Agua, S.A.U.|Method for the continuous thermal hydrolysis of organic matter, and a system suitable for carrying out said method|CN112792089A|2020-12-04|2021-05-14|杭州坤灵环境技术有限公司|Organic residue hydrolysis process|DE4230266A1|1992-09-10|1994-03-17|Bayer Ag|Method and device for heat recovery in the chemical degradation of sewage sludge or waste water|
    NO310717B1|1999-05-31|2001-08-20|Cambi As|Process and apparatus for continuous hydrolysis of wastewater|
    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:
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    优先权:
    申请号 | 申请日 | 专利标题
    ES201631577A|ES2608598B1|2016-12-13|2016-12-13|Procedure and installation for thermal hydrolysis of organic matter in steady state and with total energy recovery|ES201631577A| ES2608598B1|2016-12-13|2016-12-13|Procedure and installation for thermal hydrolysis of organic matter in steady state and with total energy recovery|
    US16/462,303| US20210017062A1|2016-12-13|2017-12-01|Method and facility for stationary thermal hydrolysis of organic material with total energy recovery|
    JP2019529983A| JP2020505216A|2016-12-13|2017-12-01|Methods and equipment for thermal hydrolysis of organic matter and total energy recovery at steady state|
    EP17885168.9A| EP3524579A4|2016-12-13|2017-12-01|Method and facility for stationary thermal hydrolysis of organic material with total energy recovery|
    PCT/ES2017/070795| WO2018115547A1|2016-12-13|2017-12-01|Method and facility for stationary thermal hydrolysis of organic material with total energy recovery|
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