DIGESTION OF ORGANIC SLUDGE

Abstract

The invention is in the field of organic sludge digestion from various sources, such as manure, sludge from a wastewater treatment plant, and an organic fraction of dredging sludge. The present method provides advanced control for serially treating aqueous organic sludge by anaerobic digestion. It further relates to dewatering of the obtained biomass.

Claims

1. A method for serially treating aqueous organic sludge by anaerobic digestion, comprising feeding input sludge through a fluidic connection to a first digestion reactor in a series of N digestion reactors and feeding a controlled part of the input sludge through a fluidic connection to a second digestion reactor, wherein N≥2, feeding an effluent of an nth digestion reactor through a fluidic connection to an n+1th digestion reactor, wherein n∈[1,N], feeding a controlled part of the effluent of a Nth digestion reactor through a fluidic connection to at least one lower ranked digestion reactor, feeding a controlled part of an effluent of the second digestion reactor through a fluidic connection to the first digestion reactor, removing a controlled part of 30-100% of the effluent of the Nth digestion reactor, obtaining concentration of fatty acids, and at least two values of pH, an amount of dry sludge in a feed, a temperature of at least one digestion reactor, and a type of the input sludge regulating a fluid level in at least one digestion reactor in the series of N digestion reactors by one of the group of limiting and preventing overflow of an nth reactor to a subsequent n+1th reactor, and a parameter selected from at least one flow, an amount of sludge in a digestion reactor, an amount of anti-foam in a digestion reactor, and combinations thereof, wherein a flow is selected from flows, and digesting the input sludge, during a period of time of more than 3 days, wherein a total solid retention time for digestion is a period of time of 3-21 days, in at least one of the series of N digestion reactors, at a temperature from 20-70° C.

2. The method according to claim 1, further comprising feeding the input sludge from the Nth digestion reactor to a post-digester.

3. The method according to claim 1, further comprising feeding a dewatering apparatus from the Nth digestion reactor and a post-digester, dewatering a formed biomass, and controlling dewatering by obtaining characteristics of the input sludge and of at least the first of the N digestion reactors and by regulating a flow between at least one Nth digestion reactor and the post-digester and the dewatering apparatus.

4. The method according to claim 3, wherein one buffers is provided before the dewatering apparatus.

5. The method according to claim 1, further comprises obtaining at least one of feed flux, production installation of input sludge, method of production of input sludge, age of input sludge, organic carbon content of input sludge, method of production of input sludge, dosing of chemicals during production of input sludge, remaining concentration of dosing chemicals left process setting during production of input sludge, polyelectrolyte concentration, type of polyelectrolyte, bowl speed, pressure applied to the sludge, gas produced, ammonium concentration in an effluent stream, concentration of proteins, concentration of sugars, concentration of cellulosic material, amount of degradable organic matter, boundary conditions during production of the input sludge, volatile fatty acid concentration, cation concentration, differential speed, and trace elements.

6. The method according to claim 1, wherein N is from 2-10.

7. The method according to claim 1, further comprising feeding a controlled part of 0-50% of the input sludge to a second digestion reactor, feeding a controlled part of 0-50% of an effluent of the second digestion reactor through a fluidic connection to the first digestion reactor, phase feeding a controlled part of 0-50% of the effluent of the first digestion reactor through a fluidic connection to at least a second digestion reactor when the effluent feedback of the Nth digestion reactor to the first digestion reactor has reached a predetermined set-point, feeding a controlled part of 0-70% of the effluent of the Nth digestion reactor through a fluidic connection to at least one lower ranked digestion reactor, feeding a controlled part of 0-30% of the effluent of the Nth digestion reactor through a fluidic connection to at least a second digestion reactor, and feeding a controlled part of 50-100% of the effluent of the Nth digestion reactor through a fluidic connection to a dewatering apparatus and to a post-digester.

8. The method according to claim 1, wherein digesting the organic sludge is in at least two digestion reactors, wherein digesting the organic sludge is in each digestion reactor independently at a temperature from 50-65° C., wherein a total solid retention time for digestion is a period of time of 4-21 days, wherein a digestion period is a combined period of at least one digestion reactor.

9. The method according to claim 1, wherein digesting is in at least one of n∈[1,N] continuous stirred tank reactors, n∈[1,N] batch reactors, a single reactor with n∈[1,N] segmented sub-reactors, and n∈[1,N] plug flow reactors.

10. The method according to claim 1, wherein the input sludge is one of manure, primary and secondary sludge from treated wastewater, and dredging; and wherein the input sludge and a digestion reactor comprises at least two different sludges.

11. (canceled)

12. The method according to claim 1, wherein dewatering is performed in at least one of a belt filter press, a centrifuge, a dewatering screw, a drum thickener, a filter press, and a gravity belt.

13. The method according to claim 1, further comprises comparing an obtained data and a predicted data from the sludge with a stored data on a server, identifying a set in the stored data which is similar to one of the group of the obtained and the predicted data, retrieving method operational settings related to the set of stored data for operating at least digestion reactor and a dewatering device, and applying at least one of the retrieved operation settings to at least digestion reactor and dewatering device.

14. The method according to claim 1, further comprises adapting at least one of pH, redox potential, volatile fatty acid concentration, alkalinity, cation concentration, and temperature, of at least one digestion reactor and dewatering device.

15. The method according to claim 1, wherein an obtained data is mathematically weighed, wherein the obtained data is mathematically averaged, and wherein a to be obtained data is mathematically predicted.

16. The method according to claim 1, wherein the method is performed continuously, at regular intervals, after an incident, or based on a statistical process control, or the combinations thereof.

17. The method according to claim 1, wherein a dry matter is measured in parallel to a fluid connection, with a radio wave device, or with an optical device, or a combination thereof; and wherein flow is controlled with one of the group of at least one valve, at least one pump, and a combination thereof.

18. (canceled)

19. The method according to claim 1, wherein during dewatering a dry matter content is measured every 0.1-2440 minutes, and wherein a dry matter content is used to adapt setting of the dewatering device.

20. The method according to claim 1, wherein the pH of at least the first digestion reactor is controlled to maintain above 5.0, wherein a redox value of at least one digestion reactor is controlled to maintain below −200 mV, wherein the pH of at least one digestion reactor is controlled to maintain below 9, wherein the redox value of at least one digestion reactor is controlled to maintain above −450 mV, wherein an amount of foam is controlled by adding 0.01-1 wt. % antifoam, and wherein the antifoam comprises a component selected from essential oils, fatty acid esters, poly alkyl glycols, alkane hydrocarbons, poly dimethyl siloxane, silicon emulsions, polyethers, silicon polymers, Simethicone, derivatives thereof, and combinations thereof.

21. The method according to claim 1, wherein an effluent of the Nth reactor is treated in a stirred tank reactor before dewatering, wherein microbial sludge is granulated, is flocculate, forms a biofilm, or a combination thereof, wherein the system is loaded with >1 kg COD, wherein at least one flow is monitored by a power consumption of a pump providing said flow, wherein aqueous sludge is pre-treated prior to feeding the input sludge through the fluidic connection to the first digestion reactor in the series of N digestion reactors, and wherein >2 kg sludge/m3 is present.

22. A reactor set-up for serially treating aqueous organic sludge by anaerobic digestion, comprising a series of N digestion reactors, wherein N≥2, between an nth digestion reactor and an n+1th digestion reactor a fluidic connection, a sludge input for a first digestion reactor, an effluent output for a Nth digestion reactor, an dewatering device in fluid connection with the post-digester, a fluidic effluent connection between a second digestion reactor and the first digestion reactor, a fluidic effluent connection between the Nth digestion reactor and at least one lower ranked digestion reactor, at least one controller for obtaining at least two values of pH, an amount of dry sludge in a feed, a temperature of at least one digestion reactor, and a type of the input sludge, wherein the at least two values are obtained from at least one of the sludge in the input and the first digestion reactor, and regulating a fluid level in a digestion reactor by one of a group of limiting or preventing overflow of an nth digestion reactor to a subsequent n+1th digestion reactor, and a parameter selected from at least one flow, an amount of sludge in a digestion reactor, an amount of anti-foam in a digestion reactor, and a combination thereof, wherein the at least one flow is selected from flows, and for controlling dewatering by obtaining values of pH and redox values, wherein the values of pH and the redox values are obtained from at least one of the sludge in the input and the first digestion reactor, and by regulating a flow between at least one Nth digestion reactor and the post-digester and the dewatering device, at least one heater for digesting the sludge in at least one digestion reactor at a temperature from 20-70° C. during a period of time of more than 3 days, and at least one pump for providing flow.

Description

DETAILED DESCRIPTION OF THE FIGURES

[0071] FIG. 1 shows schematics of a reactor set-up. 1−N reactors in series are shown, which may also relate to a reactor having 1−N compartments (lower part of the figure). This single reactor may have a curved or flat bottom, represented by the dashed line, being an alternative to the narrowing bottom. The M indicates measurements that can take place. A post-digester 11 and dewatering unit 21 are further shown. Part of the input can be directly fed to reactor 2 (dotted upper line). Part of the output of the last (Nth) reactor can be fed to a lower ranked reactor (lower dashed line). Also parts of higher ranked reactors may be fed to lower ranked reactors. This may be through a common line, or to at least one further, additional line, represented by the grayish line. Part of the second reactor can be fed back to the first reactor (solid line).

[0072] FIG. 2 shows schematics of the method of operation. Part of the contents of reactor 3 are fed back to reactor 1, and part of the contents of reactor 3 are fed back to reactors 1 and 2 respectively, typically 0-20% thereof. The pH is maintained at above 5.6. The output of reactor 3 is fed to a post-digester. The output thereof can be further treated, e.g. dewatered.

[0073] FIG. 3 shows schematically that part of the input is recirculated, part is post-digested, and part remains in the series of reactors for a given time.

[0074] The figures are further detailed in the description and examples below.

EXAMPLES/EXPERIMENTS

[0075] The below relates to an example of the present invention.

[0076] In the present invention use is made of the Ephyra® technology, which is typically applied for mesophilic processes. In this plug flow process the residence time is almost the same for all solids. This is more efficient compared to a conventional digester based on a continuous stirred tank reactor (CSTR), where a fraction of the solids has a lower residence time than the average residence time. The Ephyra® technology uses multiple compartments for digestion, therefore phase separation can take place. The phase separation causes to have mainly fatty acid production in the first compartment, therefore decreasing the pH significant in the first compartment. A recirculation flow from the last compartment is used to control the pH in the first compartment and (re)inoculation of the first compartment. There is a limit on the recirculation rate since a high recirculation rate causes the process to become more like a conventional CSTR digester. The Ephyra® concept caused an extra up to 25% of organic waste degradation, up to 25% enhanced biogas production and the capability to maintain higher loading rates, which decrease needed reactor volume. The technology also caused a better dewaterability, in turn decreasing the amount for sludge transportation. To meet demands for biosolids Class A qualification the sludge should at least comply with one of the following pathogen reduction requirements: fecal coliforms <1,000 Most Probable Number (MPN)/g Total Solids (TS) or Salmonella species <3 MPN/4 grams of TS. Next to pathogen reduction, the sludge's Volatile Solids (VS) concentration needs to be decreased with at least 38%.

[0077] Three reactors in series were used. The reactors each had a volume of 21.5 l, and were kept at 55° C. The pH was maintained in a range of 5.6-7.6 for each reactor. The first reactor typically had a lower pH than the second reactor, and the second reactor had a lower pH than the third reactor. The RT per reactor was 4 days, thus a total RT of 12 days. In practice not much difference between solid retention time and hydraulic retention time was found, if any. As starting material recirculation sludge from a thermophilic digester of a wastewater treatment plant (WWTP) in Zwolle was used. The reactors were fed with a mixture of 40% primary sludge, 60% secondary sludge, having 4 wt. % DS and 3 wt. % ODS from a WWTP in Amersfoort. Before usage the sludge was filtered with a sieve to remove large particle that could cause clogging of the tubes. The temperature, pH, DS and ODS were controlled. During the project 5 peristaltic pumps were used: 1 for the influent, 1 for the effluent, 1 for the recirculation and 1 between the first and second reactor and 1 between the second and third reactor. The pumps were set with a timer to pump 5-10 minutes every hour. The pumps were calibrated with water first, afterwards sludge was used to ensure the set point flow. To avoid acidification in the first reactor the recirculation flow was 10%. The first weeks were for starting up the reactor during which the following parameters were measured: temperature; pH; TS content; VS content. The temperature and pH were measured with corresponding sensors. The TS content was determined by drying samples in an oven at 105° C. The Volatile Solids (VS) concentration of the sludge was measured by incineration in an oven at 550° C. The temperature and pH were measured multiple times every working day. The influent's TS and VS content was measured after new sludge is retrieved from the WWTP in Amersfoort, while the effluent's TS and VS content of each reactor were measured every other working day. The TS and volatile solids (VS) were determined using crucibles and an ‘Denver Instrument Company AA-250’ analytical balance according to Standard Methods. A ‘Memmert ULM500’ oven and ‘EUROTHERM 808’ muffler furnace was used for drying and burning respectively. A “Hach HQ40D” meter was used for pH measurements. The temperature was measured with a “Voltcraft PL-125-T2”. A thermocouple was attached to the outside of each reactor and insulated with PU-foam.

[0078] The TS in reactor 3 was some 2.8 wt. %, in reactor 2 some 3.0 wt. % and in reactor 1 some 3.5 wt. %. The VS in reactor 3 was some 1.7 wt. %, in reactor 2 some 2.0 wt. % and in reactor 1 some 2.5 wt. %. Variations over time did occur.

[0079] Therein a pathogenic reduction was obtained. Coliforms were <1000 colony forming units (Mots Probable Number: MPN)/g dry matter (DS) in the effluent, salmonellas were likewise <3 MPN/g DS, and ODS digestion was >38%. The ODS reduction was best in the third reactor (some 40%), some 30% in the second reactor, and some 20% in the first reactor.

[0080] Depending of the residence time in the reactors the digestate cake had a dry solid content of >16.5 wt %.

[0081] In conclusion biosolids Class A biological matter is produced.