Patent Application
20210078890
The present disclosure relates to a method of hydrothermal carbonization of sludge, in particular municipal or industrial sludge from a wastewater treatment plant.
Sludge is typically what remains after wastewater treatment in municipal or industrial wastewater treatment plants. Municipal wastewater treatment plants treat wastewater from cities while industrial wastewater treatment plants treat water effluents from different industrial processes, for example pulp and paper mills, industrial food production facilities etc. Animal farming is also a considerable source of wastewater and sludge, for example large-scale pig farming. Embodiments of the present disclosure will be useful in all these areas.
The technologies for wastewater treatment are similar on a general level, but include specific solutions depending on the character of the waste streams to be treated, basic design, local requirements and environmental concerns. In larger plants in Sweden, the wastewater treatment process often comprises mechanical pretreatment followed by primary (settling) and secondary (aerobic) treatment steps. In some cases different forms of tertiary treatment is also applied to remove remaining problematic substances, for example drug residues, toxic organic substances etc., in the treated water. In smaller plants one or more of these stages may often be omitted.
Almost all wastewater treatment plants in use generate sludge that needs to be handled. The sludge is either recovered directly from the plant after dewatering (aerobic sludge) or first treated anaerobically for biogas production where part of the sludge is digested and the remainder is recovered as anaerobic sludge.
Wastewater treatment plants world wide produce several hundred millions metric tonnes of sludge every year and the amount is rapidly growing. In Sweden, the total sludge volume in tons of dry solids per year (tDS/y) was reported to be 250 000 in 2010 and the current figure is estimated to be the same or higher. Sludge handling is thus an enormous challenge for society, and present solutions are associated with high cost and frequently also a negative environmental impact.
Starting from 1986, the European Union has adopted several directives regulating the treatment and disposal of waste water sludge, addressing different aspects such as the use of sludge as landfill, the recovery of phosphorus, incineration of sludge etc. The various directives are reflected in national legislation in the individual member states, and for example in Sweden, the disposal of sludge in landfill has been prohibited since 2005.
Today, the main uses for wastewater sludge are fertilization in agriculture and forestry/silviculture, mixing into plant soil for ground construction projects and the coverage and restoration of landfills, incineration with energy recovery, recovery of chemicals and the production of fertilizers, and finally landfill, however provided that the sludge has undergone specific pretreatment, such as composting.
Incineration of the sludge, with energy recovery and suitable treatment of flue gases and ashes to destroy harmful chemicals and safely handle heavy metals, remains an attractive alternative. The exact composition of the sludge however depends on the composition of the incoming wastewater and the type of wastewater treatment plant. Sludge with high concentrations of organic and/or biological components is generally difficult to dewater. The water content is frequently so high that the net heating value if incinerated in a power plant is very low or even negative and the addition of support fuels, often fossil fuel, may be necessary.
C-Green Technology AB has developed a process for treatment of sludge involving a step of hydrothermal carbonization (HTC). Phosphorus can be extracted either from the biofuel before combustion or from ash after combustion.
The operation of many hydrothermal carbonization (HTC) systems require a supply of external energy, e.g. in the form of electricity or gas. The present inventors have found that the need for continuous supply of external energy in HTC treatment of sludge can be eliminated by adding an oxidation agent to a pre-heated sludge prior to the HTC reaction. The addition of the oxidation agent results in a partial wet oxidation of the sludge. The partial wet oxidation is exothermal and generates enough heat to reach the desired temperature of the HTC reaction. This simple form of oxidation is relatively easy and inexpensive to implement.
A benefit adding the oxidation agent to a preheated sludge rather than to a non-heated sludge is that a higher temperature results in a faster wet oxidation process (the rate to the wet oxidation is temperature-dependent). At temperatures above 120° C., a higher temperature also increases the solubility of oxygen gas in the sludge, which further facilitates the wet oxidation (when oxygen gas is the oxidation agent). Further, the viscosity of the sludge is substantially lower at higher temperatures, which allows for an efficient mixing with the oxidation agent.
There is thus provided a method of hydrothermal carbonization of a sludge, comprising the steps of:
a) preheating the sludge to obtain a preheated sludge;
b) adding an oxidizing agent to the preheated sludge; and
c) subjecting the sludge from step b) to hydrothermal carbonization (HTC) in a reactor to obtain a HTC-treated sludge.
The oxidizing agent is preferably oxygen gas. “Oxygen gas” refers to a gas comprising at least 80% oxygen by volume, preferably at least 95% oxygen by volume. Consequently, “adding oxygen gas” in step b) does not cover adding air (as the oxygen content of air is only 21% by volume). A benefit of using oxygen gas instead of air is that less inert gas is added to the reactor. Another benefit is a more efficient wet oxidation reaction.
As understood by the skilled person, the method is a continuous method.
The temperature of the preheated sludge to which the oxidizing agent is added in step b) is normally at least 120° C. and preferably at least 145° C., such as 145-195° C. More preferably, it is at least 150° C., such as 150-190° C. Most preferably, it is at least 165° C., such as 165-190° C.
The sludge of the present disclosure is preferably a municipal or industrial sludge from a wastewater treatment plant.
The dry solids content (also referred to as “Total Solids”) of the sludge is typically 1-35%, such as 2-35%, such as 3-32%. If the sludge is anaerobic sludge, the dry solids content is normally 13-32%. If the sludge is aerobic sludge, the dry solids content is typically 5-15%. The ash content is typically 10-75%, such as 12-50%, such as 30-50%, of the dry weight of the sludge. The higher heating value (HHV) of the sludge is typically 3.5-21 MJ/kg (dry weight), such as 6-17 MJ/kg (dry weight).
The wet oxidation of the present disclosure is partial in the sense that it does not consume the whole HHV of the sludge. Typically it consumes less than 50% of the HHV of the sludge and preferably it consumes 5-20%, such as 6-15%, of the HHV of the sludge. The amount of oxidation agent added in step b) may be adapted accordingly.
The present disclosure facilitates the separation of phosphorus (P). Accordingly, the sludge of the present disclosure preferably comprises phosphorus, e.g. in an amount of 0.5-9% of the dry weight of the sludge, such as 1-9% of the dry weight of the sludge, such as 1.5-9% of the dry weight of the sludge.
Further, the treated sludge is used as a fuel for the wet-oxidation process. The final HTC coal is also typically used as a fuel. Therefore, the sludge of the present disclosure preferably comprises carbon (C), e.g. in an amount of 9-46% of the dry weight of the sludge, such as 20-46% of the dry weight of the sludge.
The wet oxidation of the present disclosure does not require a separate reactor. Instead, it is sufficient that the fraction is mixed with the oxidation agent, e.g. using an oxygen gas mixer. Accordingly, in one embodiment, no reactor separate from the reactor of step c) is used for the reaction between the oxidizing agent and preheated sludge. The equipment needed for such an embodiment may be relatively simple and thus inexpensive. To achieve better process control, it may however be beneficial to allow the sludge to pass through a reactor for wet oxidation between step b) and step c). The retention time in such a reactor is typically shorter than the retention in the reactor of step c). For example, the retention time in the reactor for wet oxidation may be 10-60 min, such as 20-40 min. Accordingly, the volume of the reactor for wet oxidation is typically smaller than the volume of the reactor of step c). For example, the volume of the reactor for wet oxidation may be 10-50%, such as 20-40%, of the volume of the reactor of step c).
When the oxidizing agent is oxygen gas, it may be added in an amount of 60-260 kg per tonne of dry sludge processed by the method, preferably 100-200 kg per tonne of dry sludge processed by the method, more preferably 110-150 kg per tonne of dry sludge processed by the method.
The HTC-treated sludge from step c) may be cooled by flashing. Such flashing provides at least one steam fraction that is/are preferably used in the preheating of step a). In one embodiment, the flashing provides at least two, such as at least three, steam fractions of different temperatures that are used for sequential heating of the sludge in the preheating of step a).
For such an embodiment, an arrangement may be used, which arrangement comprises:
The flashing arrangement may comprise at least two, such as at least three, flashing vessels arranged in series to provide steam fractions of different temperatures. Further, the preheating arrangement may comprise at least two, such as at least three, steam mixers, such as venturi mixers, arranged in series. The steam routing arrangement preferably connects the flashing vessels to the steam mixers such that the sludge can be preheated stepwise.
The temperature of the HTC-treated sludge in step c) is 180-250° C., preferably 180-230° C. and more preferably 190-225° C.
The step of wet oxidation is carried out as the preheating is not sufficient for the sludge to reach the temperature of the HTC treatment in the reactor. The temperature of the HTC-treated sludge in step c) is normally at least 20° C. higher (such as 20-65° C. higher) and preferably at least 30° C. higher (such as 30-65° C. higher) than the temperature of the preheated sludge to which the oxidizing agent is added in step b).
The average retention time in the reactor of step c) is typically 0.25-8 h and preferably 0.5-2 h.
A first exemplary embodiment of a method according to the present disclosure is schematically illustrated in
Oxygen gas is added to the preheated sludge in an oxygen gas mixer 105 to achieve partial wet oxidation of the preheated sludge. The oxygen gas mixer is connected to an oxygen tank (not shown). The amount of oxygen gas may be about 130 kg per tonne of dry sludge processed in the system. The wet oxidation is not instantaneous. Rather, it will be ongoing when the sludge flows downstream the oxygen gas mixer 105.
After the addition of oxygen, the sludge is routed to a reactor 106 for hydrothermal carbonization (HTC) of the sludge. In an upstream section of the reactor 106, the wet oxidation reactions may be ongoing, which means that the temperature is typically lower in the upstream section of the reactor 106 than in a downstream section of the reactor 106. In the downstream section of the reactor, the temperature is typically within the range of 205-215° C.
The HTC-treated sludge from the reactor 106 is subjected to flashing in a flashing arrangement 107, which produces at least one steam fraction that is used to preheat the sludge in the preheating arrangement 101. Preferably, the flashing arrangement 107 comprises several flashing vessels arranged in series to produce steam fractions of different temperatures. For example, the flashing arrangement 107 may comprise: a first flashing vessel 108 that produces a steam fraction of relatively high temperature that is routed to the third steam mixer 104 of the preheating arrangement 101; a second flashing vessel 109 that produces a steam fraction of medium temperature that is routed to the second steam mixer 103 of the preheating arrangement 101; and a third flashing vessel 110 that produces a steam fraction of relatively low temperature that is routed to the first steam mixer 102 of the preheating arrangement 101.
The cooled slurry obtained downstream the flashing arrangement 107 is dewatered (not shown) such that at least one liquid stream (that can be used for initial heating and/or dilution of incoming sludge) and a thick fraction comprising HTC coal are obtained.
The system 100 may comprise a heater 111 using external heat, such as an electrical heater, for cold starting the process. The heater 111 is preferably arranged downstream the oxygen gas mixer, but upstream the reactor 106.
A second exemplary embodiment of a system according to the present disclosure is schematically illustrated in
Oxygen gas is added to the preheated sludge in an oxygen gas mixer 105 to achieve partial wet oxidation of the preheated sludge. The oxygen gas mixer is connected to an oxygen tank (not shown). The amount of oxygen gas may be about 130 kg per tonne of dry sludge processed in the system. The wet oxidation is not instantaneous. Therefore, a reactor 112 for wet oxidation is arranged downstream the oxygen gas mixer 105. The retention time of the sludge in such a reactor 112 may be about 30 min, which is considered to be sufficient for the wet oxidation reactions.
The temperature of the wet-oxidized sludge from the reactor 112 for wet oxidation is typically 200-215° C. This wet-oxidized sludge is routed to a reactor 106 for hydrothermal carbonization (HTC) of the sludge. The temperature may vary slightly between different positions in the HTC reactor 106 because of exothermic reactions (e.g. the HTC reactions and possibly oxidations by remaining oxygen) and heat losses. The retention time of the sludge in the HTC reactor 106 may be about 1.5 h, i.e. about three times longer than the retention time in the reactor 112 for wet oxidation. Accordingly, the volume of the HTC reactor may be three times greater than the volume of the reactor 106 for wet oxidation.
The HTC-treated sludge from the reactor 106 is subjected to flashing in a flashing arrangement 107, which produces at least one steam fraction that is used to preheat the sludge in the preheating arrangement 101. Preferably, the flashing arrangement 107 comprises several flashing vessels arranged in series to produce steam fractions of different temperatures. For example, the flashing arrangement 107 may comprise: a first flashing vessel 108 that produces a steam fraction of relatively high temperature that is routed to the third steam mixer 104 of the preheating arrangement 101; a second flashing vessel 109 that produces a steam fraction of medium temperature that is routed to the second steam mixer 103 of the preheating arrangement 101; and a third flashing vessel 110 that produces a steam fraction of relatively low temperature that is routed to the first steam mixer 102 of the preheating arrangement 101.
The cooled slurry obtained downstream the flashing arrangement 107 is dewatered (not shown) such that at least one liquid stream (that can be used for initial heating and/or dilution of incoming sludge) and a thick fraction comprising HTC coal are obtained.
The system 100 may comprise a heater 111 using external heat, such as an electrical heater, for cold starting the process. The heater 111 is preferably arranged downstream the oxygen gas mixer, but upstream the reactor 106.
| Number | Date | Country | Kind |
|---|---|---|---|
| 1751623-8 | Dec 2017 | SE | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/SE2018/051291 | 12/11/2018 | WO | 00 |
