METHOD FOR THE PRODUCTION OF BIOGAS

Abstract

A method for producing biogas in an anaerobic digestion chamber from an un-treated organic substrate, wherein said un-treated organic substrate has a dry matter of content of in the range of 20 to 90% of total solids, wherein the method comprises the steps of, pre-treatment of the un-treated organic substrate, to form a slurry having a dry matter content of in the range of 8 to 19.9% of total solids, feeding said slurry to a digestion chamber; digesting said slurry in the digestion chamber to produce biogas and a digestate, wherein in said pre-treatment step a mixture of a dilution fluid and a liquid digestate from said digestion chamber is used to dilute the un-treated organic substrate.

Claims

1. A method for producing biogas in an anaerobic digestion chamber from an un-treated organic substrate, wherein said un-treated organic substrate has a dry matter of content of in the range of 20 to 90% of total solids, wherein the method comprises the steps of: pre-treatment of the un-treated organic substrate, to form a slurry having a dry matter content of in the range of 8 to 19.9% of total solids, feeding said slurry to a digestion chamber; and digesting said slurry in the digestion chamber to produce biogas and a digestate, wherein in said pre-treatment step a mixture of a dilution fluid and a liquid digestate from said digestion chamber is used to dilute the un-treated organic substrate.

2. The method as claimed in claim 1, wherein the liquid digestate is an aerated liquid digestate.

3. The method as claimed in claim 2, wherein the liquid digestate is an aerated digestate, wherein the method further comprises aerating said liquid digestate in an aeration chamber prior to the introduction into the pre-treatment step where the digestate is aerated with any one of the gases selected from air, oxygen and nitrogen with a flow in the range of 0.1 to 100 m.sup.3 gas/m.sup.3 liquid h.

4. The method as claimed in claim 2, wherein the liquid digestate is an aerated digestate and wherein the method comprises aerating said liquid digestate prior to the introduction into the pre-treatment step during a time period of at least 1 hours.

5. The method as claimed in claim 3, wherein the viscosity of the aerated liquid digestate is decreased compared to untreated digestate during the aeration step as measured in cP.

6. The method as claimed in claim 1, wherein the liquid digestate replaces at least 5% of the dilution fluid compared to conventional methods.

7. (canceled)

8. The method of claim 2, wherein the aerated liquid digestate has a viscosity as measured cP which is lower than an untreated liquid digestate.

9. A method of cleaning an un-treated organic waste substrate prior to introduction into a biogas production facility, wherein the cleaning is performed in a hydro-cyclone, and wherein in said hydro-cyclone a cleaning liquid is used, wherein said cleaning liquid is at least partially composed of an aerated liquid digestate from a digestion chamber.

10. The method as claimed in claim 9, wherein said liquid digestate is an aerated liquid digestate.

11. The method as claimed in claim 10, wherein said aerated liquid digestate has a viscosity as measured in cP which is lower than an unaerated liquid digestate.

12. The method as claimed in claim 1, wherein the liquid digestate is an unaerated digestate.

13. The method as claimed in claim 1, wherein the liquid digestate replaces at least 25% of the dilution fluid compared to conventional methods.

14. The method as claimed in claim 1, wherein the liquid digestate replaces at least 50% of the dilution fluid compared to conventional methods.

15. The method as claimed in claim 9, wherein the liquid digestate is an unaerated digestate.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Embodiments of the present solution will now be described, by way of example, with reference to the accompanying schematic drawings.

[0030] FIG. 1 is a schematic view of a biogas production process according to the inventive idea.

[0031] FIG. 2 is a graph showing the viscosity of aerated and unaerated digestate.

[0032] FIG. 3 is a graph showing a result of a pre-hydrolysis trial.

[0033] FIG. 4 is a graph showing a result of the gas composition from trials.

[0034] FIG. 5 is a graph showing hydrogen sulfide content in the off-gases from the pre-hydrolysis step (storage of slurry).

[0035] FIG. 6 is a graph showing the specific gas production in the continuous trail.

[0036] FIG. 7 is a graph showing the amount of ammonium nitrogen in the digestion chamber.

[0037] FIG. 8 is a graph showing pH and alkalinity.

[0038] FIG. 9 is a graph showing the principle for the hydro-cyclone with water and/or aerated digestate as a liquid additive.

DESCRIPTION OF EMBODIMENTS

[0039] FIG. 1 illustrate an overview of the process. In a conventional biogas production organic waste material, such as food waste, industrial waste etc. is brought into a pre-treatment tank 1, here the waste material is pre-treated and thus mixed with dilution liquids, such as water (freshwater), or liquids from dairy or juice industry. In a facility such as the one at the Linköping municipal biogas plant about 45 000-50 000 metric tons of liquids are used annually. After the pre-treatment of the food waste, forming a slurry, the slurry usually has a dry substance content of 12-19.9%, i.e. a slurry material. The pre-treated waste is usually brought to a second step in the pre-treatment, which is at least one pasteurization chamber 1 or 2 or pre-hydrolysis chamber (storage tank for processed organic waste, slurry), wherein the pasteurization chamber 2 pathogenic microorganisms are reduced or killed. Here a certain degree of pre-hydrolysis occurs. After the pasteurization step the waste slurry material is brought to digestion chamber 3, where the waste slurry material is continuously digested under anaerobic conditions to form the gases called biogas, i.e. methane, carbon dioxide etc. The residue after digestion is called a digestate, and usually has a dry content of 3-9%. The digestate is used as a bio-fertilizer and is brought to the farmers in closed tanks, or to a treatment facility to increase the dry content. From a facility as the municipal biogas plant in Linköping, Sweden, approximately 80 000-120 000 metric tons of bio-fertilizer is produced annually, this bio-fertilizer usually has an ammonium nitrogen content of 3,000-4,000 mg/L. The farmer normally wants as high ammonium nitrogen and phosphorus content as possible. Also, the large volume of digestate to transport to the farmers is associated with a high cost.

[0040] According to one embodiment (not shown in the flow chart of the figures) of the invention a portion of the liquid digestate is brought from a digestion chamber 3 to the pre-treatment chamber 1 to replace some of the dilution liquids conventionally used in this pre-treatment step. By pre-treatment step is meant the step in the biogas process where the substrate material, i.e. undigested organic waste material of different origin is treated before it is brought to the digestion chamber.

[0041] A digestate from a digester chamber normally has a total solid (TS) content of 3-9% depending of the ingoing substrate and the degree of degradation of the material inside the digester. Moreover, the ammonium content varies depending of the substrate type, but if food waste is the main substrate the ammonium content typically is in the range of 2,000 to 4,000 mg/L (express as ammonium nitrogen).

[0042] According to an alternative embodiment of the inventive method a portion, or all, of the digestate is brought to an aeration chamber or tank 4. In the aeration chamber air is provided to flow through the digestate, thereby forming a liquid aerated digestate material. The liquid aerated digestate material has a lower dry content compared to the untreated digestate, normally in the range of 2-8% based on total solids. In FIG. 1 it is shown that all of the liquid digestate removed from the digestion chamber is brought to and aerated in the reaction chamber, however it is sufficient that only the portion needed to for dilution in the pre-treatment chamber is aerated.

[0043] The aeration may be performed, but not limited to, aeration with air, pure oxygen, and mixture of oxygen/nitrogen. In one embodiment the gas used in the reaction chamber comprises in the range of 1 to 100% O.sub.2. Normally 21% of O.sub.2 in air is used as the aeration gas. In one embodiment the flow of air in the reaction chamber is in the range of 0.1 to 100 m.sup.3 gas/m.sup.3 liquid and hour, more preferably 0.2 to 50 m.sup.3 gas/m.sup.3 liquid and hour and even more preferable 0.5 to 5 m.sup.3 gas/m.sup.3 liquid and hour.

[0044] According to one embodiment the retention time of the liquid digestate in the aeration chamber is in the range of 1 to 500 hours, more preferably 2 to 100 hours and even more preferable 12 to 48 hours. In one embodiment the retention time is at least 1 hours, or at least 2 hours.

[0045] According to this embodiment the viscosity of the aerated liquid digestate material has been reduced by at least 1%, more preferably by 10% and even more preferable by 25% compared to the untreated, i.e. not aerated liquid digestate material. This reduction of viscosity may be essential for the slurry produced in the pre-treatment step as it must have a certain viscosity for it to be fed in the system.

[0046] According to the invention around 50% of the dilution liquids can be replaced by the liquid digestate material, both untreated and treated. Preferably an aerated liquid digestate is used. A replacement of around 50% of the dilution liquids leads to a reduction of the total amount of bio-fertilizer by around 20-25% (under the conditions as set out in the municipal biogas facility in Linköping, Sweden). This results in an accumulation of ammonium nitrogen in the digestate chamber as well as in the bio-fertilizer, which in turn leads to an increase of ammonium nitrogen with about 20-25%. Thus, the water consumption decreases as well as the need for transportation of bio-fertilizer from the site to farmers land, thus providing a substantial economical saving. These amounts and improvements are all related to the specific conditions of the plant, and to the specific conditions of the raw material for the process.

Experimental Data

[0047] Trials have been performed in several different sets. The first trial set was aimed at simulating a semi-continuously fed storage tank for food waste, food waste and liquid digestate and food waste and aerate liquid digestate—naturally a pre-hydrolysis (controlled or uncontrolled) occurred when storing the slurry. In the tank a microbial culture was formed which could perform pre-hydrolysis of the slurry. The pre-hydrolysis reactors operated at a temperature of 55° C. In the second trial set both a pre-hydrolysis and a succeeding continuous biogas process for 275 days, i.e. a digestion chamber, were simulated.

[0048] In both trial sets a mixture matrix according to Table 1 were used.

TABLE-US-00001 TABLE 1 Processed Theoretic dry slurry of food contents in Food waste and Liquid Aerated the pre- waste slaughterhouse Tap untreated liquid Total hydrolysis TS = 30% waste TS = 15% water Milk Digestate digestate sum reactor Slurry 57% 33% 10% 100% 16.2% Slurry with 57%  8% 10% 25% 100% 17.3% aerated liquid digestate Slurry with 57%  8% 10% 25% 100% 17.2% liquid digestate Slurry from 75% 25% 100% 11.0% day 180 in trail 2 Slurry with 75% 25% 100% 12.3% aerated liquid digestate from day 180 in trail 2

[0049] Before the trials were initiated the viscosity of the liquid (untreated) digestate and the aerated liquid digestate (air; 24 hours, 0.5 l O.sub.2/l h; temperature 38° C.) was analyzed. These data showed that the viscosity was greatly reduced in the aerated liquid digestate, compared to the untreated liquid digestate. This surprisingly turned out to be an important effect of the aeration process, since the dilution liquid for the pre-treatment of the organic waste material, since the slurry that is formed needs a certain viscosity to be able to feed in the system. The results of the measurements are disclosed in FIG. 2. According to one embodiment the liquid digestate which is provided in the aeration chamber has a significantly lower viscosity than untreated digestate. At shear rate 50 (s.sup.−1) in this example, the viscosity drops from 41 cP down to 14 cP, a decrease with 66% compared to untreated digestate.

Pre-Hydrolysis Reactor Trials

[0050] The trial showed that the concentration of ammonium nitrogen increased when liquid digestate was reintroduced instead of using water (alone) as dilution liquid. This is due to the fact that the liquid digestate contains approximately 3,000 mg ammonium/L and water 0 mg/L. Since the liquid digestate is to be continuously reintroduced into the digestion chamber, this will have effect on the concentration of the bio-fertilizer too.

[0051] The trial showed that a certain production of gases occurred, where the gas mainly comprised carbon dioxide, and some hydrogen gas, but only trace amount of methane. On the other hand, the introduction of untreated liquid digestate lead to the occurrence of a very high concentration of hydrogen sulfide, which could be problematic due to its corrosive, toxic and inhibitive effect on materials, people and the biogas process.

[0052] When using aerated liquid digestate the hydrogen sulfide concentration or level was very low, and also significantly lower in the comparative trial with food waste handled according to the conventional process (i.e. conventional dilution fluids). There are thus several advantages by using aerated digestate as liquid to mix and dilute the organic waste with.

[0053] The trial results are shown in FIGS. 3 to 5.

[0054] Aeration of the liquid digestate leads to inhibition of the production of methane gases (which has been disclosed in the article https://www.avfallsverige.se/aktuellt/nyhetsarkiv/artikel/luftning-av-biogodsel-for-reducering-av-vaxthusgasemissioner-etapp-2/).

[0055] Aeration of the liquid digestate results in a substantial decrease in viscosity of the liquid digestate.

[0056] Mixing an aerated liquid digestate with an organic waste such as food waste or food waste slurry does not lead to any side effects with regards to the production of methane gas in the pre-treatment step, hydrogen sulfide, or other toxic or explosive gases (such as hydrogen).

[0057] Mixing of both aerated and untreated liquid digestate increases the nitrogen concentration from approximately 200 mg/L to 1000 mg/L in a pre-hydrolysis process of food waste, which leads to decrease in the amount of bio-fertilizer, which in turn leads to decrease in transportation costs, increase of value of the bio-fertilizer (as calculate based om unit volume), reduced water use, and increased energy content in the slurry for digestion.

Continuous Trials

[0058] In the continuous trial (feed once every day) the purpose was to not only simulate the pre-hydrolysis, but also to feed the formed slurry to a continuous biogas production chamber. The experiment elapsed for 275 days. All reactors where inoculated at the start with digestate from the digesters at Linköping biogas plant (Sweden). The reactors used were specially adjusted for the purpose, all described in the patent by Nordell et al (Patent SE1150954 A1). The pre-hydrolysis reactors operated at a temperature of 60° C. The digesters were operated at a temperature of 42° C. As a model plant the municipal biogas production plant of Linköping, Sweden was used. In this plant a dominating amount of food waste is used as organic material, but also some slaughterhouse waste and other minor industrial waste fractions such as fat, stillage and alcohols. The retention time was determined to 35 days in the digestion step and three (3) days in the pre-hydrolysis step (storage tank), i.e. approximately the same as in the pre-hydrolysis trial. The organic loading rate in the digesters were 4.0-4.5 kg VS/m.sup.3 day during the experiment. The first 30 days were used as start-up period were both reactors received the same slurry (food waste, milk, water). After that the experiment started and the pre-hydrolysis connected to the experiment reactor started to receive digestate in the amounts described in Table 1. After 180 days, the digestate re-circulation was replaced with aerated digestate, until day 275 when the experiment ended. When untreated digestate were used, fresh digestate from the experiment reactor were used to recirculate the same day. The aeration of the digestate from the experiment reactor took place once a week with an air flow of approximately 1 L O.sub.2/L h, T=38 C and exposure time 24 h. To facilitate the trial, the gaseous phase from the pre-hydrolysis was continuously aerated and no gas production/composition was measured. The trial was designed this way since the focus was to examine the effect on the bio-fertilizer and the stability of the process in the digestion chamber. The pre-hydrolysis reactors were fed daily with a mixture of food waste, water, milk, digestate or aerated digestate (see Table 1). And subsequently the slurry from those were fed into the digesters, one digester fed with slurry formed from food waste, water and milk; and another reactor fed with slurry formed from food waste, digestate (or aerated digestate), water and milk. A comparative trial between using an untreated and aerated liquid digestate is provided in FIGS. 6 to 8.

[0059] The trials verified that reintroducing both untreated and aerated liquid digestate results in an increase of the ammonium nitrogen content in the bio-fertilizer (and also the total nitrogen content), moreover, an up concentrations of all types of inert material, metals and mineral will of course appear in the same rate. FIG. 7. shows the ammonium nitrogen content of the digestate from the two digesters fed with different slurries. The reactor fed with slurry produced from the aerated digestate-mixture has a steady higher ammonium nitrogen content than the control. Moreover, at steady-state condition (3 retention times, or ˜105 days from the start of recirculation of digestate, thus day 135) the increase in ammonium nitrogen is 800 mg/L. The rest of the experiment showed a steady increased value of ammonium with an average increase of 850 mg/L in the experiment reactor compared to the control reactor. This corresponds to an increase with about 28% compares to the ammonium nitrogen in the control reactor (FIG. 7). There were no negative effects on the production of biogas, i.e. the production was neither increased nor decreased.

[0060] Moreover, the replacement of water with aerated digestate (or digestate) results in a higher pH, 8.0, compared to 7.8 in the control reactor (FIG. 8). This is due to the increased amount of ammonium ions which force the pH up and potentially stress the biogas process. However, the volatile fatty acids concentration was low or below the detection limit during the whole trail in both reactors (data not shown). Moreover, the increased amount of ammonium and carbonates results in a higher buffer capacity, which is desirable in a biogas process (FIG. 8).

Use of the Additive in Hydro-Cyclones to Replace Water

[0061] In some cases grit, gravel, glass etc. and heavy inert particles need to be removed from a substrate such as processed food waste (slurry) or another pumpable waste or material. The most common way to perform this is by use a hydro-cyclone that amplifies the gravidity of the heavy particles, which then can be separated from the organic waste.

EXAMPLE

[0062] At Linköping biogas plant (Linköping, Sweden) a cyclone is mounted in the circulation of the storage tank for processed food waste, the slurry. The slurry has a TS content of 14-16% in normal case. On an annual basis around 90 000 tons of slurry will pass the process. The cyclones use around 10-15 L water/min to work, resulting in 5,000 m.sup.3 water per year in consumption. Thus, the dilution of the slurry is at this plant 5-6% due to the extra water added in this step, to separate heavy inert particles such as (but not limited to) grit and gravel from the organic slurry.

[0063] The high water consumption is both a cost and dilutes the bio-fertilizer as well as shortened the retention time of the substrate in the upcoming digester. By instead using aerated digestate (and thus a liquid with low viscosity), the water consumption may be cut with 1-100% compared to the common used technique with water. Moreover, since the aerated digestate is mixed-in to a substrate flow where the grit should be separated, there is of greatest importance to avoid gas bubbles and gas formation. Since the aerated digestate lacks dissolved methane and has low content of carbon dioxide this is a suitable liquid. Finally, the aerated digestate has a low viscosity, which is a requirement to be able to use the digestate as a counter flow in the cyclone. By using aerated digestate in the cyclone, dilution can be avoided as the aerated digestate contains high amount of nitrogen and phosphorus etc. which is desirable in the bio-fertilizer. Even more positively, this cuts the amount of transports needed to transport the bio-fertilizer to the farmers at the end of the process. See FIG. 9.