The production of olives destined for the oil supply chain has undergone profound changes over the years, which mainly concern:

• The increase in production yields per unit area.
• The reduction of unit production costs through mechanization.
• The need to adapt to changes in the collection and cultivation by-products.
• The trend towards industrialization of the sector.

Currently, the olive cultivation systems for the oil supply chain divides into traditional and modern. The density in traditional systems does not exceed 200 trees/ha, while in modern ones, it can reach up to 2000 trees/ha [56]. A further difference is that traditional olive groves are on marginal lands or in the edges of lands intended for other crops. In contrast, modern systems are dedicated plantations, equipped with irrigation systems, and designed to mechanize harvesting, pruning, and residual biomass collection [35,36,37,40,55,56,57]. The usual classification considers high density (HD) and super high density (SHD) systems.

Traditional olive groves cover an area of 8–9 Mha worldwide, while modern ones cover just over 3 Mha [58]. Of these, 82% is covered by HD cultivation systems and the remainder, about 0.5 Mha, by SHD systems [59]. Faced with this situation, modern olive groves’ production per unit area is considerably higher.

The new plants built outside Europe are all modern, HD and SHD. In Europe, the conversion is also proceeding with public contributions. In Portugal, modern systems now account for 64% of the total. At the same time, in Morocco, about 46% of traditional olive groves are being transformed into modern HD and more than 9% into SHD orchards. Overall, the transformation of traditional olive groves into modern ones is proceeding at a rate of 1.5% per year of the area concerned (Olive Time 2020). Figure 2 and Figure 3 show this situation related to 2016/2017 campaign with more additional information.

As already mentioned, details on the arrangement of plants in HD and SHD olives growth are given in many books and manuals while the most used cultivars are reported, among others, by Paul Vossen [10]. Before concluding this paragraph, it is worth citing and briefly discussing two recent publications on the ongoing research activities. One of these [60] examines a new type of intensive olive grove called pedestrian orchards, proposed as an alternative to current HD and SHD systems since it could further reduce production costs and enhance the quality, functional properties, and typicality of the oil produced, simultaneously reducing environmental impact. The other [56] examines the problem of mulching with lignocellulosic material (leaves and pruning) resulting from the maintenance of modern SHD plants. The experimentation activity implies high costs and long times for both these aspects. Furthermore, the validation of the results is possible after an adequate number of oil campaigns.

In order to produce high-quality oil, the olives must be harvested without breaking the skin, and the fruit should be processed within 12 to 24 h. Fruit should be separated by quality, with each grade processed separately [57,61]. Oil from olives is separated mechanically, unlike what happens for other fruits, seeds, and vegetables in general. First, however, it is necessary to carry out some of the upstream operations, in particular:

• Washing, carried out with water to remove any residues of pesticides and woody and inorganic debris. Leaves, dust, and other light debris are removed in advance by blowing air.
• Grinding, generally carried out discontinuously with stone crushers or continuously, using modern hammer mills, toothed discs, and cylindrical or roller crushers. The grinding aims to break and crush the fruit to allow the separation of liquids trapped in the solid matrix [57,62,63,64].
• Malaxation, consisting in stirring, slowly and gently, the material obtained from the grinding to aggregate the oil dispersed between the aqueous and solid phases in drops for subsequent separation. Malaxation lasts about an hour, during which it is necessary to avoid the oxidation of polyphenols and control the release of volatile compounds that affect the olfactory quality of the final product [65]. For this purpose, modern machines are hermetic and allowed to operate in a controlled atmosphere or under a vacuum. Other modern measures concern light and rapid heating of the dough with non-traditional technologies and possibly the preventive de-stoning of the olives [66,67,68,69,70].

Once completed upstream treatments, the paste is sent to the plants to separate the oily phase from the solids and VW. The traditional technologies used for this operation are the traditional press and, rarely, selective filtration or percolation (Sinolea process), which are discontinuous processes [57,71], now used only for small productions or for lots of precious olives destined for the production, in limited quantities, of oils with special characteristics and very high costs. Numerous texts and manuals concerning the production of olive oil describe the details of this process and related equipment used. Percolation has meagre extraction yields. It is strongly dependent on the percolation duration and the ratio between oil and water, typical of processed olives [10,57]. For the sake of completeness, it is worth mentioning another technology considered at the laboratory level to separate oil from olive paste after all upstream treatments. This technology, widely used in the food industry, employs supercritical CO₂ as a separation medium [72,73]. Strictly speaking, the oil obtained in this way could not be labelled as virgin or extra virgin oil, but it would have all the characteristics of such oil as the non-toxic CO₂ is entirely removable by decompression of the supercritical phase.

Since the early 1960s, continuous separation by centrifugation has been placed on the market and adopted at an increasing rate. For about 30 years, the three-phase decanter has been used to separate the pulp from the malaxation process into three phases: a wet solid (pomace), an aqueous phase, VW, and the organic liquid phase (virgin olive oil or extra virgin olive oil). This technology involves adding hot water to the olive paste with the inevitable consequence of increasing the flow of VW and the complex environmental problems associated with the difficulty of purifying this aqueous waste. At the beginning of the 1990s, the marketing and use of the two-phase decanter began at an increasing rate. In this case, it is not necessary to add water to the pasta fed to the decanter. The heart of both these technologies lies in the horizontal decanter, where the upstreamed olives undergo centrifugal action at about 3000 rpm [74].

In the three-phase system, the added water washes away some of the flavours and antioxidants and results in lower polyphenol content in the oil. In a two-phase system, the decanter has only two outlets: one for the oil and one for the wetted pomace. With the two-phase decanter, it is possible to reduce drastically or eliminate the production of the very polluting wastewater, thus solving the significant problem of the disposal of VW that has afflicted the olive oil industry for so many years. Furthermore, the extraction yield is improved compared to the batch mills, while the oil quality is comparable or even better [75]. The oily phase produced by the centrifuge must be further processed to eliminate the tiny amount of water and the few solids that make the oil cloudy and affect its sensory and organoleptic characteristics. For this purpose, a vertical centrifuge is used, which, at the same rpm, can exert a greater separation force [76,77,78,79]. Figure 4 graphically shows the various stages of the virgin (VO) or extra virgin (EVOO) olive oil production process.

The clarified oil goes to downstream operations:

• Weighing.
• Temporary storage in stainless steel barrels.
• Final packaging in glass or metal containers (labelled and ready for marketing).

In the case of low-quality raw material, the downstream operations are more complex as they must foresee some refining process.

Figure 5 [51] shows the material balance for the traditional batch mill and the two continuous three-phase and two-phase centrifugal systems.

It is worth emphasizing that the two-phase system is based on the observation that the pomace produced by a traditional batch mill can be mixed with the corresponding VW to obtain a single wetted solid phase. For the same reason, the three-phase decanter is easily transformable into a two-phase decanter by recycling the VW stream, as shown in Figure 6. It would also be better to introduce a membrane filtration system (microfiltration of VW and Reverse Osmosis of the permeate) with very high concentration factors (15–20) to recycle a purified solution and recombine the small amount of retentate with the pomace. In this case, the quality of the oil produced would be practically identical to that of the three-phase decanter. However, the cost of reconversion, periodic regeneration of membranes, replacement of filter modules, and energy consumption would increase operating costs in a non-marginal way.

A new decanter, called DMF or Multi-Phase Decanter (MPD), has recently been developed and adopted by some sizeable Italian oil mills. It represents the evolution of the two-phase decanter. MPD does not require any addition of water for the malaxation phase. In addition, the oily phase produces a solid phase, like that obtained with the three-phase decanter and a further pitted solid-phase called paté. The olive paté has a humidity similar to or higher than that of the pomace produced by the two-phase decanter and contains, in significant concentration, numerous substances with high nutritional and functional power to be used as a basis for the preparation of food for human use, with dietary-therapeutic and diet-preventive characteristics [34,80,81]. Figure 7 summarizes the MPD material balance.

It is not possible to foresee the commercial development of the MDP and the olive paté. It is not easy to involve Spain and the other countries that have recently adopted the two-phase decanter technology. It is also challenging to think of a simple transformation of the two-phase decanter into MPD. However, should the paté become a widely consumed product, MPD could spread massively. In addition, the pomace produced by MPD has a much higher energy content as it contains all the woody parts of the kernel. The percentage of residual oil tends to decrease with introducing new technologies upstream and downstream of the malaxation process. The recombination of the pomace from the batch mill with the polluting VW was not practiced in the past, for two reasons principally: the environmental regulation was less stringent for VW purification before discharging, and the pomace was further processed by drying followed by solvent extraction, to recover the residual amount of oil (about 5–6%). Some decade ago, the solvent extraction of the olive pomace started to become obsolete in many major olive oil producer countries. For example, in Italy, most olive pomace oil extraction plants were dismissed, and almost the same happened in Spain, where the adoption of the two-phase system was subsidized by public funding. In the USA, there does not exist any olive pomace oil extraction plants [10].

From all the above, it is reasonable to assume that soon the OMW will be made only of SOMW. This significant milestone for the olive oil industry allows to avoid the problem, never solved, related to the VW management, and discourages using pomace to recover residual oil by solvent extraction [32,82,83,84,85,86,87,88]. Unlike in the past, the very wet SOMW is unsuitable as a by-product. Instead, it represents an actual waste to be purified, possibly through energy enhancement or recovery of matter and energy. Furthermore, woody waste from pruning and leaves from the olives pretreatment could be treated along with SOMW in a context in which the oil sector takes on the characteristics of an agro-industrial activity.

In some cases, a precious by-product is a woody material deriving from the pitting of the olives. This material, produced in minimal quantities compared to SOMW and TCW, is typically used to produce high-quality activated carbon, characterized by a very high adsorbing surface (micropores) per unit of mass. Finally, simple membrane filtration operations allow recovering and recycling the olive washing water.

Anaerobic digestion (AD) is a consolidated and widely applied, all around the world, full-scale technology for the disposal of a variety of biomass waste such as the manure produced by livestock farms, excess sludge produced by urban wastewater treatment plants, food and agro-industrial waste, and the wet fraction deriving from the separate collection of municipal solid waste [89,90]. AD occurs in the absence of oxygen and at atmospheric pressure. Depending on the type of microorganisms used, mesophilic or thermophilic, the operating temperature is between 40 and 60 °C, respectively.

AD with mesophilic bacteria is the most used even if it requires longer residence times, 7–30 days depending on the characteristics of the treated material (liquid, semi-solid and solid), the type of reactor (mixing or flow piston), and the type of process (continuous or batch). AD is usually divided into hydrolysis, acidogenesis, acetogenesis, and methanogenesis. AD products are Biogas rich in methane (typically 50–70%), carbon dioxide, and other substances at low concentrations, such as water vapour. Burning Biogas allows producing electrical energy and heat. In large plants (over one hundred thousand t/a of raw material), removing the inert part from the Biogas may be convenient to transform it into renewable methane to be used as a substitute for natural gas in both gaseous and liquid form. The other typical effluents of AD are the digestate sludge, consisting of the wetted solid part of the feed more resistant to attack by microorganisms, and process water. The final disposal of both digestate and wastewater depends on the type of treated material and the plant’s context [91]. The application of AD to olive oil mills waste has been extensively studied since these materials are very rich in organic matter that is mainly biodegradable [92,93,94,95,96,97,98]. However, it does not apply to lignocellulosic residues, such as pruning and olive pits. A further and not marginal problem is the high concentration of aromatic compounds and lipids, which are toxic for methanogenic bacteria. A recently published paper analyzes in detail the problems related with the application of AD to OMW generated by three phase decanters in Saudi Arabia concluding that pretreatment and co-digestion are crucial factor to obtain satisfactory results [99].

AD involves high investment costs and is economically inapplicable when the plant’s potential is less than a few tens of thousands of tons per year [91,100,101]. Waste from oil mills can be treated with this technology only if added in a limited percentage (10–20%) to different substrates for which AD is the preferred solution [102,103]. Alternatively, they require previous pretreatments to eliminate or transform bactericidal substances [94,104,105,106,107]. Further alternatives are the adoption of technology solutions that allow reducing the feed flow rate of the incoming biomass and its stratification, considering that the total input solids are variable during the processing time [108] and the hybridization of AD with pyrolysis [109]. When treating OMW with AD and the manure deriving from animal breeding, the digestate can find application as a soil improver, even if the woody fragments deriving from the crushing of the stone can have negative implications in the medium–long term [27]. The application of AD to the final disposal of SOMW presents several contraindications of both a technical and regulation nature. Co-AD and process integration are more promising. Achieving economic feasibility is not easy.

Composting is a term universally used to identify the solid-phase fermentation of biodegradable organic materials in excess of oxygen. Using uncontaminated materials such a treatment is a typical example of waste to a valuable product called compost. Compost has fascinating characteristics for use in the agronomic field, like horticulture, gardening, and ornamental plants for indoor and outdoor use. Otherwise, an off-specification compost is obtained. It is usually landfilled as a stabilized substance that does not produce leachate. The agronomic properties of compost depend on the presence of humic acids and fulvic acids that perform a soil amendment action, supporting the intense stimulation of microbial activity in the soil and the plant’s ability to absorb fertilizing elements present in the soil or added with fertilization. Good conditions for the life of microorganisms require a humidity between 40% and 60%, and optimal C/N ratio between 25 and 30 and must contain both Phosphorus and Potassium. The composting process splits into two phases after adjusting the composition and particle size of the mixture. The first is bio-oxidation, which takes place in about seven days, while the second is maturation which takes a few months. During the first phase, the temperature of the mass of material tends to increase up to 60–70 °C due to exothermic reactions with the consequent killing of pathogenic microorganisms. This phase is carried out in batch or continuous reactors, equipped with ventilation systems and temperature monitoring of the solid mass and filtering systems to prevent the escape of malodorous gaseous substances. The maturation has the purpose of stabilizing and containing compost before packaging and marketing (for compost to specification) or landfilling (for compost out of specification). The application of this technology for the treatment of SOMW has received much attention [110,111,112,113,114,115,116], and there are numerous full-scale applications. Like AD, SOMW composting must account for the presence of bactericidal substances and the need to adjust moisture and nutrient ratios using other biodegradable organic materials through composting. Also, in contrast to AD, SOMW composting does not produce but consumes electricity, primarily for aeration of the solid mass during bio-oxidation. Compared to AD, the size of the composting plants is not limiting. The conduction is more manageable than in AD, and the material obtained is more stabilized. Usually, the compost value does not repay the investment and production costs. A further problem of composting is the one deriving from the production of unrecoverable CO₂, being diluted in excess air. Like for AD, the final disposal of SOMW by composting is problematic. Co-composting is mandatory and process integration can give more chances to this widely diffused and easily applicable technology. Economic feasibility is not easily achievable.

Conventional thermal treatments of waste rich in organic material are torrefaction, pyrolysis, gasification, and combustion. The list is made in ascending order of operating temperature ranging from about 150 °C for torrefaction to over 1000 °C for combustion. Research and technological development activities, including recent ones, on applying heat treatments to SOMW are widely documented [43,50,117,118,119,120,121,122,123,124,125,126,127,128,129,130,131,132,133,134,135,136,137,138]. Heat treatments are all aimed at the disposal of SOMW with the concomitant recovery of the energy contained in them. More specifically, torrefaction and pyrolysis occur at atmospheric pressure and without oxygen. In the former, the material is heated to 150–300 °C using, generally, a part of the product of torrefaction that has the characteristics of solid semi-carbonaceous fuel, devoid of volatile organic substances and with residual humidity tending to zero. Subsequently, the product thus obtained is aggregated into pellets by extrusion or other geometric shapes using, for this purpose, other technologies and compression equipment.

The purpose of aggregation is to eliminate dust formation and increase the density of the solid fuel, thus favouring its use. In addition to the pressure effect, aggregation is favoured by the formation, during treatment, of small quantities of bituminous material that acts as glue. The torrefaction of SOMW is not applied on an industrial scale because it is energetically and environmentally unsustainable; this happens because of the high humidity of the charge and the presence of volatile compounds with high contaminating power in the atmosphere. Pyrolysis or carbonization instead is realized by previously heating the material to a sufficiently high temperature (about 280 °C) to cause the breakage of the heavy organic molecules and trigger a series of exothermic reactions capable of achieving further heating of the mass up to 500–600 °C. Under these conditions, one obtains practically anhydrous coal and high energy density representing the main product. At the same time, a gas is produced that contains all the water initially present in the feed, the volatile organic substances and the less volatile ones resulting from the thermal splitting of the larger molecules into coal, and compounds that at room temperature have a bituminous appearance [139,140]. When the moisture content of the feedstock is not excessively high, the combustion of the gaseous phase may be sufficient to support the endothermic phase of the pyrolysis process. At the same time, it supports the elimination of a gaseous effluent that should be recondensed to avoid atmospheric pollution. Subsequently, it should be separated into an aqueous liquid phase with high contaminating power and an organic phase with rheological characteristics that strongly limit its use as a fuel. In other words, when the moisture content of the feedstock does not exceed 25–35%, the pyrolysis process is energetically self-sufficient, and the pyrolysis product is a valuable solid material mainly used to replace fossil coal. Therefore, pyrolysation of SOMW is not attractive for full-scale applications. In contrast, both torrefaction and pyrolysis can apply well to the energy densification of TCW.

However, pelletization after natural ground drying and shredding is generally preferred. In this regard, it is worth pointing out that wood pellets are the solid fuel with the largest market share in Europe and that pruning’s waste is the preferred raw material for its production [27]. This is due to the size that facilitates its natural moisture reduction and the ease of shredding. At temperatures higher than those used for pyrolysis (600–800 °C) and in a partially oxidizing environment, the thermal treatment of biomass is generally called gasification [141,142] and the product of this operation is called Syngas. It is a mixture of H₂ and CO used as a renewable fuel and a fundamental building block for many hydrocarbons. The conversion of Syngas into fuels for power generation or motor fuels and chemicals has been widely described in many scientific papers mentioned earlier and in books [143]. Similar considerations as for pyrolysis apply to the gasification of SOMW and TCW. Direct combustion of biomass for energy production is undoubtedly the most widespread technology applied at full scale. Combustion requires excess oxygen at temperatures between 800 and over 1000 °C, depending on the composition of the feed (moisture content and type of inorganic compounds), size of material, and type of combustor. The application of direct combustion to SOMW is practically impossible due to the moisture content, which is incompatible with the ignition temperature. The chlorine content is another critical contraindication for the direct combustion of SOMW, even in mixtures with other materials [54]. Elevated hydrogen chloride emissions from biomass combustion in utility boilers are a significant issue. They can cause corrosion problems and deposit molten alkali chloride salts on boiler’s water tubes, resulting in further corrosion and the possible formation of very polluting compounds. Pyrolysis is a good pre-treatment for solving this problem [144].

The hydrothermal technologies allow transforming biomass into solid, liquid, or gaseous fuels in an aqueous environment. If the product is a carbonaceous solid, the familiar name of the process is hydrothermal carbonization (HTC). Similarly, we refer to hydrothermal liquefaction (HTL) if the product is an organic liquid. The most advanced in terms of full-scale application of the two processes is HTC. It takes place in a reactor at temperatures ranging from 180 to 250 °C, under autogenous pressure (approximately the vapour pressure of water at the operating temperature), residence time ranging from 0.5 to 8 h, and optimal weight ratio between water and organic compound in the range between 5 and 10. It is widely agreed that the HTC process imitates the coalification (brown coal formation process) within a few hours, which takes place in nature over enormously longer geological periods of 50,000–50 million years. It was described in 1913 [145] and recently reconsidered by [146,147,148,149]. Multiple reactions occur during the HTC process, namely hydrolysis, dehydration, decarboxylation, and aromatization.

A small quantity of gas, mainly CO₂ (about 1% of the dry organic biomass processed), evolves during the HTC treatment. It is discharged into the atmosphere after purification by adsorption or washing. Consequently, both the ratios hydrogen to carbon (H/C) and oxygen to carbon (O/C) decrease, giving rise to a carbon-rich hydrochar separated from the process water by filtration or centrifugation. The overall yield of hydrochar, on a dry basis, varies over a wide range (30–70%) depending on the nature of the biomass processed and the upstream treatments, temperature, residence time, reactor type, the ratio of water to biomass, and pH. HTC is an exothermic process releasing 25–38% of the dry biomass’s energy value, resulting in a significant improvement of the energy balance of the whole process.

The application of HTC for the disposal and valorization of wet and very wet waste biomass from the agri-food industry, livestock farming, biological purification of urban wastewater, algae and other dedicated crops on non-marginal land has been the subject of research, technological development, modelling, and development of processes and plants at the pilot, pre-industrial and, in some cases, industrial scales by numerous researchers, public and private bodies and entrepreneurs. Recent scientific works made by the authors of this review are a testimony to this and, at the same time, a source of information [148,149,150,151,152,153]. On the other hand, this review reports the most recent works and reviews concerning the research activities on the application of HTC to olive oil production wastes and by-products regarding SOMW produced by the two-phase decanter and TCW and solid mixtures of these and other biomasses [154,155,156,157,158,159,160,161]. In Figure 8, a continuous HTC process with heat recovery for hydrochar (HC) production from wet and very wet waste biomass, including the two-phase decanter SOMW, TCW, and mixtures thereof, is schematically presented.

If the material to be processed has a moisture content of 65%, typical for SOMW, at 200 °C, a residence time of one hour and a water/SOMW ratio on a dry basis of 7.5, approximately 27% mechanically dehydrated HC with a residual moisture content of 30% is obtained. The possibility of mechanically dehydrating HC to such low levels depends on the hydrophobic characteristics and the small grain size of the solid material obtained from the treatment. It is worth noting that HC, with all residual moisture, has a mass almost four times lower than SOMW. It is entirely biologically stable as it is sterilized and has solid fuel characteristics in ignition temperature and energy content. The amount of process water remaining from the treatment is comparable to that of the AV produced by traditional olive oil mills. Unlike AV, it is sterilized and has about five times lower COD values as it does not contain carbohydrates, fats, and suspended solids. Compared to AV, the process water from SOMW’s HTC treatment is much more suitable for fertigation, both in odour pollution and for a lower concentration of substances with bactericidal power. Similar but more favourable considerations apply to the HTC treatment of TCW or mixtures of SOMW and TCW. The energy balance and the waste-to-energy value of the HTC treatment of SOMW can derive from the following considerations. 80% of the heat required to bring the feed to reaction temperature is recovered from the process water, while direct contact condensation of steam at 225 °C gives the remaining required heat. Approximately 10% of the energy content of the dry biomass fed to the plant is lost as water-soluble organic compounds, while the remainder remains in the HC. Under the specified operating conditions, about three tons of aqueous suspension must be heated for each ton of feed. The net heat from isothermal reactions and losses, burning no more than 5–10% of the HC, produces the energy required by the HTC process. The remainder can be used for electricity production, heating, as a carbonaceous material with adsorbent properties, for soil improvement, and other applications [162,163]. As already mentioned, a different hydrothermal technology for the treatment and valorization of wet and very wet biomass, such as SOMW, is the liquefaction of the organic fraction under supercritical water conditions [135,164]. The very severe operating conditions of pressure and temperature make these technologies less attractive than HTC for full-scale applications. For the sake of completeness, it is worth adding that supercritical water treatment of biomass, including SOMW, can also be done in an oxidizing atmosphere [43], in contrast to HTL. In this case, the process is called supercritical water oxidation. It has been the subject of much attention at the laboratory and pilot plant research level, mainly to destroy very toxic organic substances dissolved or dispersed in water at low concentrations [165,166,167].

Process integration is the interconnection of two or more technologies to minimize energy consumption, limit environmental impact, and diversify the products obtainable from processing raw materials and their by-products and waste. Biorefinery is a different way of indicating process integration. It prefigures the possibility of treating SOMW to obtain, from renewable organic material, a variety of chemicals traditionally produced using raw materials of fossil origin. In the context of the oil sector, this approach has been the subject of intense research and technological development for the treatment of SOMW and TCW. For example, Schievano et al. proposed an integrated biorefinery concept to manage pomace, using SFE for extracting polyphenols and fatty acids, followed by the thermochemical recovery of energy, biofuels, and materials [168]. Plaza et al. proposed the production of Hydroxytyrosol from solid OMW using deep eutectic solvents and then supercritical CO₂ [169]. Similarly, other researchers have proposed this approach to produce new materials, with sometimes unpredictable destinations, integrating partly established and partly innovative technologies usually used in other sectors [46,156,162,170,171,172,173,174,175,176,177,178]. However, although attractive, process integration and biorefining involve higher investment costs and organizational and commercial complications. It is necessary to assess the economic feasibility of this approach on a case-by-case basis and define the limits of integration in terms of both technologies and products. Another non-marginal aspect concerns territorial, business, and raw material integration. This aspect of the problem can be better clarified by referring to the treatment of SOMW, TCW and other possible by-products and waste from olive oil production.

A typical example is a pomace oil extraction plant that recovers oil from pomace by solvent extraction. Such plants serve a much larger territory than individual olive groves and receive pomace from numerous mills. Moreover, several pomace oil extraction plants deliver the extracted oil to a refining plant that processes oil extracted from different fruits and seeds. Similarly, the size of the SOMW treatment plant is generally not compatible with the farm size, and a single treatment technology might not be the optimal choice to valorize woody wastes such as TCW, together with SOMW. A process integration that seems interesting could be a hybrid consisting of one section of HTC, one of AD, and one of filtration with semi-permeable membranes. In this case, the HTC pre-treatment of the lignocellulosic material produces HC and contributes to increasing biogas production by the AD. The membrane filtration section could treat all wastewater, including washing water. However, there remains the problem of seasonality that is typical of all processes and plants in the agro-industrial sector. For this reason, there is no generalized solution. However, a hybrid process such as the one briefly described and a census of the biomass availability during the year could significantly contribute to sustainable development, according to the EU Taxonomy [179].