PROCESS FOR THE DISPOSAL OF SOLID OR LIQUID WASTES FROM TREATMENT OF ANIMAL SOURCE MATERIALS

Abstract: Process for the disposal of solid or liquid wastes deriving from treatment operations of animal source materials, like lime baths or waste liquors from the processing of fish or meat or hides, with the recovery of useful or recyclable substances like sodium chloride and a peptide concentrate, and the release of purified waste liquors.

Description: PROCESS FOR THE DISPOSAL OF SOLID WASTES FROM TREATMENT OF ANIMAL SOURCE MATERIALS DESCRIPTION Field of the invention The present invention relates to a process for the disposal of solid or liquid wastes deriving from treatment operations of animal source materials, particularly those that have been subjected to treatments with common salt (sodium chloride) for preservation or other aims. Examples of sucn residues are those deriving from lime baths, soaking or desalting liquors, and in case from other sol d- or liquid-phase tanning residues, as well as liquors loaαed with organic matter deriving from fish processing plants, like tuna, anchovies offal ana the like, as well as from meat processing plants, like cutchery, tinning, feedstuff residues and the like. The process according to the present invention allows to eliminate the dumping of highly polluting wastes, finally yielding three products: a solid product useful in agriculture, a peptide concentrate, useful m the agricultural and in the industrial field or destined to thermal destruction as alternative fuel, and salt (sodium cnloride), reusable anew in the industrial processes, such as, e.g., in the hide tanning process. Prior art As it is known, with particular reference to the hide processing industry, prior to the tanning steps the hides are beaten for salt recovery, then subjected to a soaking or desalting treatment with possible further wasnmgs, and subsequently subjected to a so-called «lιme bath» (BDC) treatment in a markedly alkaline environment and using sodium sulphide and other substances, m order to ease the subsequent tanning steps, thus improving the final tannage quality. The liquor outlet from the lime baths is highly polluted in terms of COD, ranging from 15.000 to 40.000 mg/1, sulphides, ranging from 1.500 to 5.000 mg/1, and /05707 - 2 - chlorides, ranging from 20.000 to 50.000 mg/1, and it is drained, after a possible separation of the solid phases 'like, e.g., the undissolved hair), in the purifier of the tanning plant itself or channeled to an external purifier, m order to be subjected to chemical-physical and iological purification treatments . Currently adopted purification treatment methods provide the mere filtration with the recovery of the sulphur ion-containing liquors, the ultraflltration, or, pore simply, the acidification with acids, like sulphuric acid or hydrochloric acid, at a pH 3-6 (isoelectric point of the proteins contained in the lime pits), with or without neating, for a variable time and the subsequent filtration with recovery of an organic residue. However, such treatment methods merely allow a reduction of the COD, of the TKN for the protein precipitation, the sulphide abatement, the water clarification, and, hence, only partially overcome the problems entailed in the lime pit purification; in particular, to date the problem entailed by the presence of high COD, TKN and chlorides, as well as the disposal of the resulting sludge, has not been overcome. Moreover, several drawbacks and problems, entailed in tie presence of the soaking, desalting, and lime liquors, and possioly of other washing liquors deriving from this first tanning stage, crop up during the purification treatment. Hereinafter such liquors will be referred to as «3DC». Among these drawbacks, a difficulty in the biological purification needs to be mentioned, due to the high amount of organic charge to be disposed, with the consequent accumulation of remarkable sludge amounts, as well as to the presence of significant sulphide amounts, tnat can entail problems, both oαorous and of sulphate increase m the drained liquors. The possible precipitation of not easily filterable metal sulpmdes entails further difficulties for a regular f ltratio . 1/05707 - 3 - Moreover, apparently the presence in high percentages of chlorides in the BDCs that are in no way separated during the chemical-physical and biological liquor purification treatment can yield a high chloride concentration also in the purified liquors themselves, causing the «chloπdes» parameter to exceed the limit values set by the waste disposal provisions, thereby remarkably worsening the management of the entire purification plant. Finally, other difficulties are caused by the direct draining of the BDCs into the purifier, e.g. the possible presence in the latter of bactericidal substances that obviously could inactivate the biological plant. As already highlighted, also other drained liquors, deriving from the processing of materials of animal origin, including fish, nave high contents of protein organic matter and of salts. Therefore, difficulties for the purification plants of such liquors might ensue, as the chloride concentration, not abated by the purification process, may exceed the legal limits set for the dumping of the purified liquors. Description of the Invention For the sake of simplicity, n the following description particular reference will be made to the problems and to the overcoming of the problems related to lime pits, as a representative example of suitable material in a process according to the invention. To a person skilled in the art it will be apparent that also other waste materials highly polluted by organic residues and by sodium chloride could be treated according to the present invention . An object of the present invention is that of implementing a process synergistically operating chemically and physically through BDCs treatment steps in order to recover products useful in the agricultural, livestock and industrial field. Among those, there are e.g. the clarification plasters, used as calcium so l conditioners /05707 - 4 - for agriculture, or thermally treated as deriving from, and containing, proteins of animal origin, sterilized peptide concentrates useful in the livestock, agricultural or industrial field or possioly useful as alternative fuel for the production of steam reusaϋle within the same manufacturing process, and, lastly and better characterizing the invention, a salt, sodium chloride (NaCl), obtained tnrough the crystallization and the subsequent refining steps, to be used in the industrial field n general, and specifically to be recycled m the tanning plants during the pickling step. A further object of the present invention, in the case of tanning plant wastes, is that of implementing a process in which not merely the BDCs as such, but also the BDCs admixed with the washing liquors used in the lime baths, as well as with all the offal of animal origin possibly pre- treated and considered as residues or wastes by the tanning plants themselves or by companies operating in the field of the wastes of animal origin, l ke, e.g., fleshing, limed pieces, hair, tanning residues, as well as other treatable wastes of animal origin. In that case, the BDCs themselves, as well as the BDCs admixed with any wastes of animal origin whatsoever are classified as «wastes of animal oπgιn», therefore subject to the current European and Italian provisions . Those objects are attained on one hand by applying to wastes of animal origin nydrolysis and chemical-physical separation processes, and, on the other hand, physical processes of ultraflltration and reverse osmosis and/or evaporation, crystallization and refining of the sodium chloride, yielding a reusable protein concentrate and the sodium chloride, reusable as well. Such processes synergistically integrate thereamong, finally resulting not only in a waste liquor αramable in the known way, out also in recyclable products useful n the agricultural, livestock or thermal energy production fields, or even within the plant processing the material of an ma- origin itself, with an advantage in cost-effectiveness. Operationally, the process according to the invention consists of two stages: a first stage, hereinafter referred to as «stage 1», comprising BDC treatment steps, developable through several technological paths, with the ultimate object of: recovering peptide and/or inorganic sludge, destined to agricultural or industrial use, recovering the hydrogen sulphide in its various end products (sulphuric acid, to be reused in the steps of said stage 1 or possibly to be sold, ammonium sulphide, sodium bisulphite, calcium sulphate, sodium sulphide or sodium sulphydrate possibly recoverable in the tanning operations, etc.) and producing a saline peptide liquor that is subsequently subjected to a second stage, the «stage 2». In this second stage tne peptide concentrate and the sodium chloride are recovered by ultraflltration and reverse osmosis and/or evaporation, salt crystallization and refining processes, all obviously to be construed as an unitary production process. Hence, the object of the present invention is a process for the disposal of solid or liquid wastes deriving from treatment steps of materials of animal origin, said wastes containing protein products of animal origin and saline products, yielding environmentally disposable waste liquors and industrially useful recovery products, characterized in that it comprises, in a first stage, the steps of: hydrolyzmg said protein products in order to obtain a saline peptide liquor; purifying said peptide liquor from solids and Calcium and Sulphur compounds; and m a second stage consecutive to said first stage, the steps of: separating the industrially useful sodium chloride from said peptide liquor and obtaining a treatable peptide byproduct useful in the agricultural or livestock field, or as fuel; the waste liquors having an extremely low pollutant residual content after said two treatment steps, can be delivered to a stanαard purification plant or directly to the dumping site. - 6 - A more specific object of the present invention is a process wherein said first treatment stage comprises the steps of: accumulating said protein products of animal origin in an aqueous saline suspension; hydrolyzmg said suspension, continuously or in batches, m a markedly alkaline environment under conditions ranging from room temperature and atmospheric pressure to 160°C and under pressure in order to obtain said peptide liquor; separating the soliαs contained inside said liquor; decalcifying said liquor by reaction with carbon dioxide or other carbonates or bicarbonates for producing calcium carbonate; and separating the calcium carbonate from said liquor at a 5-11 pH, in order to ootam a limpid peptide liquor to feed to said second stage. More specifically, the second stage comprises the steps of: concentrating said saline peptide _ιquor by evaporation of a quantity of the solution water sufficient to obtain a pre-concentrate in which the salt concentration does not exceed that at the crystallization start; crystallizing the salt by a further solution water removal from said peptide liquor; and separating the crystallized salt from the peptide liquor in order to obtain said salt and said peptide concentrate. Brief description of the drawings Those and other features of the present invention will oe better highlighted through the description, given merely oy way of example and without limitative purposes, of five application examples, four thereof experimental and carried cut in a laboratory and one thereof applicative of an industrial scale process, and with reference to the annexed drawings, wherein: - Figures 1 to 4 depict, according to a block diagram, four different operational ways for carrying out the first stage of the process according to tne invention; Figures 5 and 6 depict, according to a block d_agram, two different operational ways for carrying out tie second stage of the process according to the invention; and Figure 7 sketches a plant for carrying out the process according to the invention. Embodiments of the Invention Description of the first stage, or «stage 1», of the process according to the invention: To date, tne art is aware of several methods leading to the recovery of a peptide and/or inorganic sludge, to the recovery of the developed hydrogen sulphide and to the production of a saline peptide liquor. Four such methods, selected among the most significant and economically feasible for the purpose, will hereinafter be described. First way to carry out the «stage 1» of the process. With reference to the block diagram of Fig. 1, the following sequential steps are illustrated: a) accumulating the possibly admixed BDCs, with the salt recovered by hide beating, or already present in the BDCs themselves in case the beating step can be avoided in the tanning plant, with the recovered hair possibly already present- m the BDCs themselves, both dissolved or suspended, with other wastes of animal origin deriving from the tanning steps, or possibly from other steps, even unrelated to the tanning industry (e.g. meat flours, etc.) b) hydrolyzmg the BDCs, to which the suspension is fed into the reactor m batches, as well as continuously, where, exploiting the markedly alkaline environment of the BDCs themselves or casewise adding an alkali compound, a high temperature treatment under pressure is carried out (taking into account the existing laws in the field of animal origin waste processing, a 133°C 2 min 3 bar treatment can be envisaged; however, the hydrolysis process can possibly be carried out also at room temperature and not under pressure, lengthening at will the processing times thereof) . c) Separating the solids, after the hydrolysis treatment the alkali turbid is fed to a solid separation step (lime, calcium sulphate, traces of undissolved hair, etc.), in which the thermally treated peptide liquor, and /05707 subsequently, provided the steps are carried out according to the existing provisions concerning wastes cf animal origin, sterilized as well, proceeds to the s_r>sequent treatment, whereas the separated solid is fed to a possible pressing and drying process. d) Decalcifying the peptide liquor, the liquor yielded by the process c) is fed into specific reactors m which carbon dioxide or other carbonates or bicarbonates are added m order to obtain calcium carbonate recoverable by itself or admixable to the previously oDtamed solids. This step is obtainable under hot as well as cold conditions. The step can be completed, before or after the calcium carbonate separating step, lowering the pH to 5-3 by the addition of ivdrochloric acid or other suitable acids (preferably hyαrochloπc acid, as it produces recoverable sodium chloride) and with a subsequent air or Nitrogen scrubbing in order to completely develop the solution sulphides as hydrogen sulphide. The latter step (air or Nitrogen scrubbing) can also be carried out without acid addition. Such steps can be subsequent to the calcium carbonate separation, therefore operating onto the limpid saline liquor, as highlighted in the block diagram of FIG. 1. e) Separating the calcium carbonate, the turbid with a 5-11 pH (average 7-8) is fed to a separation step of the calcium carbonate, that can be pressed and dried to be sold as such or admixed to the solid obtained from process c) and then casewise pressed and/or dried and sola in the agricultural field as soil conditioner or additive. This solid can also have livestock and industrial uses. The decalcified peptide liquor is accumulated and it is ready for stage 2 of the process ooject of the invention herein disclosed . f) hydrogen sulphide treating, the gaseous flow containing the hydrogen sulphiαe of which at d) is subjected to suitable treatments aimed at the recovery thereof as sulohuπc acid, calcium sulphate, ammonium /05707 sulphide, sodium bisulphite, sodium sulphide or sodium sulphydrate, etc. Second way to carry out the «stage 1» of the process. With reference to the bloc diagram of FIG. 2, the following sequential steps are illustrated: a : accumulating the possibly admixed BDCs, with the salt recovered by hide beating cr already present in the BDCs tnemselves in case the beating step can be avoided in the tanning plant, with the recovery hair that can already be present in the BDC themselves both dissolved or suspended, with other wastes of animal origin deriving from the tanning steps or possibly from other steps, even unrelated to the tanning industry (e.g., meat flours, etc. ) . b) Hydrolyzing the BDCs, in which the suspension is reactor fed in batches as well as continuously, where, exploiting the markedly alkaline environment of the BDCs themselves or casewise adding an alkali compound, a high temperature treatment under pressure is carried out (taking into account the existing laws in the field of the animal origin waste processing, a 133°C 2 mm 3 bar treatment can be envisaged; however, the hydrolysis process can possibly be carried out also at room temperature and not under pressure, lengthening the processing times at will). c) acid treatment of the turbid, after the hydrolysis treatment, the alkali turbid is acidified with sulphuric acid or other m such an amount to lower the turbid pH to 0-6. The step can be carried out under hot or cold conditions, lasting for the time required for the elimination of the sulphides present m the solution as hydrogen sulphide. The step can ce completed with the air or Nitrogen scrubbing in order to completely develop as hydrogen sulphide the sulphides present in the solution. d) Alkali treatment of the turbid, the acidic turbid yielded from c) is treated with l me milk or other alkali compounα in order to precipitate the previously added sulphuric acid or other as sulphate or other. This step can oe carried out under hot or cold conditions (as acid in the standard process sulphuric acid is used, and lime as base, ..n order to obtain calcium sulphate, precipitating under iigh temperatures, mere traces thereof being left n the solution; moreover, the calcium sulphate is widely used in agriculture or in the industrial field) . e) Separating the solids, after the treatment of which at d) the alkali turbid is fed to a solid separation step lime, calcium sulphate, traces of undissolved hair, etc.), _n which the thermally treated, and subsequently, provided the steps are carried out according to the existing provisions regarding wastes of animal origin, sterilized as /ell, proceeds to the subsequent treatment, whereas the separated solid is fed to a possible pressing and drying process . f) Decalcifying the peptide liquor, the liquor yielded from process e) is fed into specific reactors in which carbon dioxide or other carbonates or bicarbonates is added _n order to obtain recoverable calcium carbonate by itself or admixable to the previously obtained solids. This step can be carried out under hot or cold conditions. g) Separating the calcium carbonate, the turbid with a 5-8 pH (average 7-8) is fed to a separation step of the calcium carbonate that can be pressed and dried to be sold as such or admixed to the solid yielded by e) and then casewise pressed and/or dried and sold as soil conditioner cr additive in the agricultural field. This solid can also -ave livestock and industrial uses. The decalcified peptide _ιquor is accumulated and it is ready for stage 2 of the process object of the invention herein disclosed. h) Hydrogen sulphide treating, The gaseous flow containing the hydrogen sulphide of which at d) is Ξ b ecteα to suitable treatments aimed at the recovery t h ereof as sulphuric acid, calcium sulphate, ammonium sulphide, sodium oisulphite, sodium sulphide or sodium s_lphydrate, etc. Third way to carry out the «stage 1» of the process. With reference to the block diagram di FIG. 3, the following sequential steps are illustrated: a) accumulating the possibly admixed BDCs, with the salt recovered by hide beating or already present in the BDCs themselves in case the beating step can be avoided m the tanning plant, with the recovered hair that can already be present in the BDC themselves both dissolved or suspended, with other wastes of animal origin deriving from the tanning steps or possibly from other steps, even unrelated to the tanning industry (e.g. meat flours, etc.) b) Oxidizing the sulphides, the sulphides dissolved in the BDCs are oxidized to thiosulphates and/or sulphates with a suitable oxidizing agent (e.g., hydrogen dioxide, pure oxygen, sodium hypochlorite, etc.) casewise adopting suitable catalysts. The temperature and the length of the process are functions of the oxidizing agent used. c) Hydrolyzmg the BDCs, in which the suspension is fed to reactors in batches as well as continuously, where, exploiting the markedly alkali environment of the BDCs themselves or casewise adding an alkali compound, a high temperature treatment under pressure is carried out (taking into account the existing laws n the field of animal origin waste processing a 133°C 2 mm 3 bar treatment can be envisaged; however, the hydrolysis process can possibly be carried out also at room temperature and not under pressure, lengthening the processing times thereof at will) . d) Separating the solids, after the hydrolysis treatment the alkali turbid is fed to a solid separation step (lime, calcium sulphate, traces of undissolved hair, etc.), in which the thermally treated peptide liquor, and subsequently, provided the steps are carried out according to the existing provisions regarding wastes of animal origin, sterilized as well, proceeds to the subsequent treatment, whereas the separated solid is fed to a possible pressing and drying process. e) Decalcifying the peptide liquor, the liquor yielded by the process d) is fed into specific reactors n which carbon dioxide or other carbonates o bicarbonates is added in order to obtain calcium carbonate recoverable oy itself or admixable to the previously obtained solids. This step s obtainable under hot as well as cold conditions. f) Separating tne calcium carbonate, the turoid with a 5-8 pή (average 7-8) is fed to a separation step of the calcium carbonate tnat can be pressed and dried to be sold as such or admixed to tne solid yielded by b) and then casewise pressed and/or dried and sold in the agricultural field as soil conditioner or additive. This solid can also have livestock and industrial uses . The decalcified peptide liquor is accumulated and it is ready for stage 2 of the process object of the invention herein disclosed. Fourth way to carry out the «stage 1» of the process. With reference to the block diagram n FIG. 4, the following sequential steps are illustrated: a) accumulating the possibly admixed BDCs, with the salt recovered by hide beating or already present in the BDCs themselves in case the beating step can be avoided in the tanning plant, with the recovered hair that can already be present in the BDC themselves both dissolved or suspended, with other wastes of animal origin deriving from the tanning steps or possioly from other steps, even unrelated to the tanning industry (e.g. meat flours, etc.) . b) Acidically treating the BDCs, the BDCs are acidified with an amount of sulphuric acid or other sufficient to lower the pH to 3-6 (isoelectric point of the collagen proteins, that gelify while precipitating) . The step lasts for a time required for the elimination of the sulphides present in the solution as hydrogen sulpnide and it can be carried out under hot or cold conditions. The step can be completed with the injection of air or Nitrogen in order to completely develop as hydrogen sulphide the sulphides present in the solution (hot conditions are more expensive, however the subsequent solid separation step is greatly eased thereby) c) Separating the solids, after the treatment of which at b) the acidic turbid is fed to a solid separation step (undissolved and gel protein, calcium sulphate, traces of undissolved hair, etc.), in which the protein liquor passes to the subsequent hydrolyz g treatment, whereas the separated solid is fed to a thermal sterilization process, of which at l ) . d) Hydrolyzmg treatment of the protein liquor, wmch the liquor is fed to reactors in batches as well as continuously, where, casewise adding a further amount of acidic compound or an amount of an alkali compound sufficient to basify the liquor, a high temperature treatment under pressure is carried out (taking into account tne existing laws m the field of the animal origin waste processing a 20 mm 133°C 3 bar treatment can be envisageα; however, the hydrolysis process can possibly be carried out also at room temperature and not under pressure, lengthening the processing times thereof at will) . e) Separating the solids for a second time, after the hydrolysis treatment, the liquor or the turbid is fed to a solid separation step (calcium sulphate, etc.), in which the protein liquor passes to the subsequent decalcification treatment, whereas the separated solid is fed to a possible thermal drying process, of which at ) . f) Decalcifying the peptide liquor, the liquor yielded by the process e) is fed into specific reactors into which carbon dioxide or other carbonates o bicarbonates is added in order to obtain calcium carbonate, recoverable by itself or admixable to the previously obtained solids. This step can be carried out under hot as well as cold conditions. g) Separating the calcium carbonate, the 5-11 pH (average 7-8) turbid is fed to separation step of the calcium carbonate that can be pressed and dried to be sold as such or admixed to the solid ootamed by e) and then casewise pressed and/or αried and sold in the agricultural field as soil conditioner or additive. This solid can also /05707 - 14 - nave livestock and industrial uses. The decalcified peptide liquor is accumulated and it is ready for stage 2 of the process object of the invention herein disclosed. h) Treating the hydrogen sulphide, the gaseous flow containing the nydrogen sulphide of wnicn at b) is subjected to suitable treatments aimed at the recovery thereof as sulphuric acid, calcium sulphate, ammonium sulphide, sodium bisulphite, sodium sulphide or sodium sulphydrate, etc. l) Thermally treating the protein solid, the protein solid yielded by c), casewise admixed to the other solids separated during the process steps, is subjected to a thermal sterilization treatment according to the existing provisions for tne agricultural or industrial field (e.g., a 133°C treatment for 20 mm under pressure) . ) Solid drying, the solids yielded by the thermal treatment process I) , casewise admixed to the other solids separated during the process steps, are subsequently dried order to obtain a stable product, salable in the agricultural or industrial field. Description of the second stage, or «stage 2» of the process according to the invention: To date, the art is aware of several recovery methods yielding a 80-100% pure sodium chloride and a hydrolyzed peptide that can be subsequently treated for the production of several finished products for the livestock, agricultural or industrial field, or utilized as such in the above-mentioned fields, or, lastly, utilized as alternative fuel for the production of steam or electric energy, recovering the salt contained therein or not. Hereinafter, the process that, applied to the saline peptide liquor obtained stage 1, leads to the sodium c.iloride crystallization and purification and to the yield cf the peptide concentrate, as shown in the diagrams of FIGS. 5-6. The saline liquor can be treated in an ultraflltration aid/or osmosis plant for pre-concentrat g the saline phase, increasing its chloride concentration from about 30- 35 g/1 to about 45-55 g/1. The initial liquor is concentrated 1.5-2 times with the known techniques and the laboratory tests, then it can be delivered to a subsequent concentration and final crystallization step, or directly delivered to the crystallization step (cf. FIG. 6 Diagram). However, the salt cannot be entirely recovered by this system, as a portion thereof will remain in the permeate due to the ultraflltration and/or osmosis step (on average, a waste liquor containing about 300-1000 mg/1 chlorides, equal to 1/3 of the treated liquors, is obtained) . The peptide concentrate disclosed hereinafter could be utilized in a special liquid waste incinerator as alternative fuel for the production of steam, to be used in the steps of the above-disclosed process or m the evaporation stage; the salt yielded by the combustion process will again be water-dissolved and treated together The water drained from the evaporation and crystallization process will be treated m a special plant m order to allow the direct dumping thereof, complying with the limits set by the existing laws. With reference to the block diagram of FIGS. 5-6, the following sequential steps are illustrated: a) concentration, the saline peptide liquor could be pre-concentrated in a ultraflltration and/or osmosis plant as already disclosed; the saline peptide liquor is pre- concentrated into a multi-effect concentrator that thermally or mechanically compresses the steam in order to optimize the cost of this step. Special care should be paid during the above-described process in order to avoid an excessive smearing or scaling of the mam concentrator, arresting the former when a pre-concentrate still free of salt crystals is obtained. Apparently, such an evaporating step could also be carried out with a single apparatus, however the existing technology suggests to carry it out according to two separate substeps. b) First crystallization, the pre-concentrate is fed to a evaporation crystallization plant (a cooling crystallization plant is conceivable, however the technology most suited to the material subjected to the process suggests to carry out the crystallization process oy evaporation; a single crystallization process could be used, yielding a high-quality salt, having however an excessive content of final saline peptide concentrate: hence a double crystallization is suggested. c) Separating the salt, the crystallized salt is separated from peptide concentrate by a centrifugation or a filtration process. The peptide concentrate can be sold as such or utilized as an alternative source of energy, e.g., for the production of steam, whereas the yielded salt is washed with a brine, in case additioned with oxidizers (e.g., hydrogen dioxide) to eliminate the residual sulphide traces m order to obtain the purified salt, that is then αelivered to the drying and storing process. The brine is redelivered to the crystallization process for the salt and the peptide concentrate recovery. d) Second crystallization, the peptide concentrate yielded by centrifuging or filtering the crystallized salt can be subjected to a second crystallization for a further salt recovery, thereby reducing the final peptide concentrate. e) Purification of the drained liquors, the drained liquors derived from the evaporation and crystallization process are admixed and delivered to a purification plant for allowing the direct dumping thereof in compliance with tne existing provisions. This purification plant consists of a stripping treatment of the solubilized ammonia, of a second treatment step with hydrogen dioxide or other oxidizer m order to eliminate the residual sulpnide traces, finally percolating it through an activated charcoal layer, m order to reduce the COD withm lawful limits . Various analyses carrieα out onto the _ιquors deriving from the concentration and crystallization process have assessed the above-described processes to amply suffice to make the waste liquors fall withm • lawful parameters . Application examples of the process of the invention Appl i ca tion exampl e n . 1 . The application example 1 relates to a laboratory tes . 10.000 g BDC were processed according to the process αiscloseα hereinafter, with the following analytical results : • COD = 37.420 mg/1 • TKNf = 2.195 mg/1 • Sulphides = 3.109 mg/1 • Chlorides = 25.000 mg/1 About 2% b/w recovered salt and aoout 3% b/w recovered hair were added to this BDC (these percentages derive from an examination of the amounts of recovered salt and hair usually separable from the BDCs drained m the waste liquors of a tanning plant) . Apparently, this waste should be considered as a waste of animal origin, although extremely diluted m a water solution or suspension, because the partially dissolved or suspended protein is already classified as such; moreover, the end result of such steps _s a peptide concentrate useful n the industrial, livestock and agricultural fields . The process disclosed hereinafter results from the synergy of stage 1, carried out according to the steps shown m the diagram of FIG. 1 and stage 2, as shown in the diagram of FIG. 5. 200 g recovered salt and 300 g recovered hair were added to an amount equal to 10.000 g BDC drained from a tanning plant . The suspension was subjected to a thermal hydrolysis treatment under pressure, at 150°C and at a pressure of about 5 bar for 30 mm. The treated suspension is cooleα to about 80°C and vacuum-filtered by buchner. The saline peptide liquor is treated, at 70°C, with gaseous carbon dioxide, in order to precipitate the calcium as calcium caroonate. The carbon dioxide scrubbing is carried out to pH 8. Due to the pH decrease, the sulphides develop as hydrogen sulphide. In order to complete the development tnereof, a pure Nitrogen scrubbing is carried out for 15 mm after the carbon dioxide scrubbing (no recovery of the developed hydrogen sulphide was carried out) The suspension thus obtained is vacuum-filtered by buchner . The separated calcium carbonate is added to the solid separated during the first filtration. Therefore, about 270 g dry solid are obtained. Then the saline peptide liquor is treated, according to what provided by stage 2. The saline peptide liquor is pre- concentrated and the first thermal crystallization is carried out by rotary evaporator ( thermostatic bath temperature = 70°C, steam temperature about 40°C, vacuum equal to 75 cm Hg) . The pre-concentration is carried on until the concentrate assumes a honey-like texture (there are suspended sodium chloride crystals) and about 80% of the water is evaporated. Then a first vacuum filtration is carried out by ouchner . The concentrate is further subjected to rotary evaporator crystallization until about 50% of the residual ater is evaporated. The vacuum filtration by buchner is repeated, and the raw salt yielded by the first filtration is admixed to that yielded by the second filtration. The raw salt is purified by washings with a sodium cnloride/hydroge dioxide saturated brine. Thus, about 560 g sodium chloride and about 400 g 60% cry peptide concentrate are obtained. The liquors yielded from the analyzed concentration and crystallization steps had the following analytical values : • COD = 112 mg/1 • TKN = 7 mg/1 • Chlorides = absent • Sulphates = absent • Sulphides < 1 mg/1 Applica tion example n . 2. The application example n. 2 relates to a laboratory test . 10.000 g BDC were treated according to the process disclosed hereinafter, with the following analysis: • COD = 40.520 mg/1 • TKNf = 1.670 mg/1 • Sulphides = 2.208 mg/1 • Chlorides = 39.500 mg/1 About 2% b/w recovered salt and about 3% b/w recovered hair were added to this BDC (these percentages derive from an examination of the amounts of recovered salt and hair that are usually separated from the BDCs drained in the waste liquors of a tanning plant) . Apparently, this waste should be considered as a waste of animal origin, although extremely diluted m a water solution or suspension, because the partially dissolved or suspended protein is already classified as such; moreover, the end result of such steps is a peptide concentrate useful in the industrial, livestock and agricultural fields . The process disclosed hereinafter results from the synergy of stage 1, carried out according to the steps shown in the diagram of FIG. 1 and stage 2, as shown in the diagram of FIG. 5. 200 g recovered salt and 300 g recovered hair were added to an amount equal to 10.000 g BDC drained from a tanning plant. The suspension was subjected to a thermal hydrolysis treatment under pressure, at 150°C and at a pressure of about 5 bar for 1 hour. The treated suspension is cooled to about 85°C and vacuum-filtered by buchner. The saline peptide liquor is treated, at 85°C, with sodium Dicarbonate in order to precipitate the calcium as calcium carbonate. The suspension thus obtained is vacuum-filtered by buchner . The separated calcium carbonate is added to the solid separated in the first filtration. Therefore, about 270 g dry solid are obtained. Then, 37% hydrochloric ac d is added to tne saline peptiαe liquor, maintained at 85 C C, until lowering the pH to about 7 (0.8% hydrochloric acid is utilized on the BDCs) . Due to the pH decrease, the sulphides develop as hydrogen sulphide. In order to ease the development thereof, a pure Nitrogen scrubbing is carried out for 30 mm (no recovery of the developed hydrogen sulphide was carried out) . Then, the saline peptide liquor is treated according to what provided by stage 2. The saline peptide liquor is pre-concentrated and tne first thermal crystallization is carπeα out by rotary evaporator ( thermostatic bath temperature = 70°C, steam temperature = about 40°C, vacuum equal to 75 cm Hg) . The pre-concentration is carried on until the concentrate assumes a honey-like texture (there are suspended sodium chloride crystals) and about 80% of the water is evaporated. Then a first vacuum filtration is carried out oy bucnner . The concentrate is further subjected to a rotary evaporator crystallization until aoout 50% of the residual water is evaporated. The vacuum filtration oy buchner is repeated, and the raw salt yielded by the first filtration is admixed to that yielded by the second filtration. The raw salt is purified by washings with a sodium chloride saturated brine. Thus, about 500 g sodium chloride and about 380 g 60% dry peptide concentrate are obtained. The liquors deriving from the analyzed concentration and crystallization steps had the following analytical values : • COD = <10 mg/1 • TKN = 5 mg/1 • Chlorides = absent • Sulphates = absent • Sulphides < 1 mg/1 Appl i ca tion example n . 3. The process disclosed hereinafter, shown m the diagram of FIG. 7, results from the synergy of stage 1, carried out according to the steps shown in the diagram of FIG. 1 and stage 2, as shown in the diagram of FIG. 5. Always n such process, reference is made to the processing of 1.000 t BDC with the addition of about 20 t recovereα salt and about 30 t recovered hair (the BDC is delivered to the processing plants with suitable vehicles) . The entire suspended product is stored inside accumulation tanks Tl, of a capacity allowing the BDC homogenizing and a storage thereof equal to 3 working days, so as to take into account possible plant maintenance steps. The BDCs are fed, with the process pump PCI, to the heat exchanger El, inside which they are heated to about 100°C, carrying out a thermal recovery from the hydrolysis step under continuous pressure. The neated BDCs are fed to the sequential reactors Rl and R2 , allowing to carry out the hydrolysis process at 145°C, under a pressure of about 6 bar, for an average permanence time of about 30 mm (these conditions allow a good alkaline hydrolysis of the dissolved and undissolved proteins like, e.g., the hair, as well as the thorough dissolving of the suspended salt) . The treated BDCs suspension is fed to the container 71, where the flash due to the expansion to atmospheric pressure takes place (an evaporation takes place at this stage and the resulting gases and the emitted steams are conveyed to the final incinerator plant) . The suspension is fed, with the process pump PC2, to the decanter DC1, in which the separation of the solid phase made of calcium sulphate and lime m excess with possible traces of proteins undissolved from the hydrolyzed peptide liquor takes place. The peptide liquor is fed, with the process pump PC3, to the reactor R3, in which carbon dioxide is additioned, tnrough a special bottom scrubber, at about 70-80 c C. The carbon dioxide addition is controlled by the process pHmeter inserted in the reactor, and the process is considered to be over when the pH decreases from about 11 to about 8, m order not to develop soluble calcium bicarbonate . Due to the carbon dioxide addition and to the pH decrease, the hydrogen sulphide develops from the reactor R3 (such hydrogen sulphide is further developed by a final hot air or steam scrubbing) . This hydrogen sulphide is fed to a combustion plant, inside which it is transformed into sulphur dioxide, that is then absorbed n a specific aosorption tower with calcium carbonate; then the yielded calcium sulphite is oxidized to calcium sulphate by air and/or oxygen scrubbing. About 14 t 70% dry calcium sulphate (that can be admixed to the subsequently filtered solids, or sold as chemical plaster to companies utilizing such materials) are yielded by this process. Anyhow, the flue gases of the sulphide recovery plant are delivered to the final incineration plant . After the combustion process leading to S02 formation, such gaseous flow can also be fed to a sulphuric acid oroduction plant, obtaining a product that can easily be sold or treated in other sulphates or sulphites production plants . The peptide liquor containing the calcium carbonate is fed, with the process pump PC4, to the decanter DC2 , where tne calcium carbonate is separated from the saline peptide _ιquor . The solid inlet by tne decanter DC1 through the pump PM1 and the solid inlet oy the decanter DC2 through the pump PM2 are delivered to a mixer MX1, hydrogen dioxide being fed therein m order to oxidize to calcium sulphate the residual sulphides. From this mixer, through the pump PM3, the suspension containing about 25% dry matter is delivered to a press filter FI, yielding a saline peptide liquor that is redelivered to the decanter DC2, and a solid, having about 70% ory matter, that is directly sold to the companies operating in the agricultural field. (The yielded dry solid equals about 35 t, having approximately 15% S03, 20% CaO, 1.5% Norg, therefore constituting a satisfactory clarification plaster, salable as soil conditioner in the agricultural field. The saline peptide liquor inlet from the process pump PC5 is fed to a five-effect thermally compressed evaporation plant EV1. Therein, the about 950 t of initial liquor with a dry content equal to about 8.5-9.0% is brought to the sodium chloride crystallization start, and therefore to about 40% of the dry content (thus, a water amount equal to about 700-750 t is evaporated, with a steam consumption equal to about 6.5-7.0 t/hour. The pre-concentrate is fed to the accumulation tank V2 , and therefrom it is fed to the crystallization plant CR1, through the pump PC6. This plant is of the forced- circulation type, with steam thermal compression for the thermal recovery withm the heat exchanger of the plant itself . The crystallized suspension is directly fed to the ribbon filter F2 for the separation step of the saline peptide concentrate, that is accumulated in the tank T3 (yield = about 50 t) and then sold in the livestock, agricultural or industrial field, from the crystallized salt, that is washed counter-current with a saturated sodium chloride solution previously prepared and stored in the tank T2. The saline washing liquors are directly delivered to the crystallization plant CR1. The crystallized and purified salt is finally dried inside the final section of the same ribbon filter, yielding about 55 t dry salt of 93-98% pureness, directly reusable in the tanning plants. Applica tion example n . 4. The application example n. 4 relates to a laboratory test. 10.000 g of liquors deriving from fish processing (like, e.g., tuna, anchovies offal, etc.), hereinafter referred to as ALP, were processed according to the process hereinafter disclosed, with the following analytical values : • COD = 27.995 mg/1 • TKN f = 2.500 mg/1 • Chlorides = 62.100 mg/1 The final result of the purification steps of these liquors is a peptide concentrate useful in the industrial, livestock and agricultural fields, or possibly as an alternative fuel for the production of steam to be used withm the process itself. The process disclosed hereinafter results from the synergy of stage 1, carried out according to the steps shown n the diagram di FIG. 1 (due to the lack of sulphur ions in the ALP no acidic treatment of the peptide liquor is carried out) and stage 2, as shown in the diagram of fig . 6. An amount equal to 10.000 g ALP drained from a tuna processing plant, additioned with 400 g hydrated lime, was subjected to a thermal hydrolysis treatment under pressure at 145°C and under a pressure of about 4 bar for 1 hour. The treated suspension s cooled to about 85°C and vacuum-filtered by buchner. The salme peptide liquor is treated, at 85°C, with controlled pH carbon dioxide, m order to precipitate the calcium as calcium carbonate. The suspension thus obtained is vacuum-filtered by buchner . The separated calcium carbonate is added to the solid separated m the first filtration. Thus, about 540 g dry solid are obtained. Then, the salme peptide liquor is treated according to what provided by stage 2. The salme peptide liquor is pre-concentrated and the first thermal crystallization is carried out oy rotary evaporator ( thermostatic bath temperature = 70°C, steam temperature aoout 40°C, vacuum equal to 75 cm Hg) . The pre-concentration is carried on until the concentrate assumes a honey-like texture (there are suspended sodium chloride crystals) and about 80% of the water is evaporated. Then a first vacuum filtration is carried out by buchner . The concentrate is further subjected to rotary evaporator crystallization until about 50% of the residual water is evaporated. The vacuum filtration by buchner is repeated, and the raw salt yielded by the first filtration is admixed to that yielded by the second filtration. The raw salt is purified by washings with a sodium chloride saturated brine. Thus, about 600 g sodium chloride and about 320 g 60% dry peptide concentrate are obtained. The liquors deriving from the analyzed concentration and crystallization steps had the following analytical values : • COD = <I0 mg/1 • TKN = 8 mg/1 • Chlorides = absent Then the peptide concentrate is demineralized by percolating it through ion exchange resms . In order to be demmeralized, the peptide concentrate is first diluted into 320 g water to obtain a dry matter concentration equal to the 30 %. The yielded liquor is percolated through ultraflltration membranes (thus resulting further diluted until having a dry matter content equal to about the 20%) and then through a cathode exchange column and through an anionic exchange column. Then, the demmeralized peptide liquor is concentrated again. About 210 g final concentrate are obtained, characterized by an organic nitrogen content equal to 8.5%, a dry matter content equal to 60% and absence of ashes. This concentrate is of high value, salable m the industrial, agricultural and livestock fields . Appl i ca ti ve exampl e n . 5 . The applicative example n.5 relates to a laboratory test . 10.000 g of liquors deriving from the processing of mammal butchery residues for the production of meat flours (hereinafter referred to as AFCs) were processed according to the process disclosed hereinafter, with the following analytical values : • COD = 35.300 mg/1 • TKN f = 5.500 mg/1 • Chlorides = 27.000 mg/1 The end result of the processing steps of these liquors is a peptide concentrate useful m the industrial, livestock and agricultural fields, or as alternative fuel for the production of steam to be used withm the process itself. The process disclosed hereinafter results from the synergy of stage 1, carried out according to the steps shown in the diagram of FIG. 1 (stage (C) is not carried out: a single solid separation (E) is carried out after the calcium abatement treatment (D)) and stage 2, as disclosed in the diagram of FIG. 5. An amount equal to 10.000 g AFC drained from a meat flour production plant, additioned with 400 g hydrated lime, was subjected to a thermal hydrolysis treatment under pressure at 145°C and under about 4 bar for 1 hour. The treated suspension is cooled to about 85°C and it is treated with controlled pH carbon dioxide, m order to precipitate the calcium as calcium carbonate. The suspension thus obtained is vacuum-filtered by buchner. About 450 g dry solid matter are obtained. Then the salme peptide liquor is treated, according to what provided in stage 2. The salme peptide liquor is pre-concentrated and the first thermal crystallization is carried out by rotary evaporator ( thermostatic bath temperature 70°C, steam temperature about 40°C, vacuum equal to 75 cm Hg) . The pre-concentration is carried out until the concentrate assumes a honey-like texture (there are suspended sodium chloride crystals) and about 80% of the water is evaporated. Then a first vacuum filtration is carried out by buchner. The concentrate is further subjected to rotary evaporator crystallization until about 50% of the residual water is evaporated. The vacuum filtration by buchner is repeated, and the raw salt yielded by the first filtration is admixed to that yielded by the second filtration. The raw salt is purified by washings with a sodium chloride saturated brine. Thus, about 450 g sodium chloride and about 400 g, 65% dry, peptide concentrate are obtained. The liquors deriving from the concentration and crystallization steps had the following analytical values: • COD = <10 mg/1 • TKN = 6 mg/1 • Chlorides = absent Industrial applicability From what has hereto been disclosed, it is apparent now the opject of the invention was fully attained where, operating synergistically, the exclusion from the chemical- physical and biological purification treatments was attained for the BDCs or the analogous organic matter salme baths of a substantially protein nature, also obtaining a cost-effective recovery due to the production of recyclable end products, as well as drastically eliminating materials that are highly polluting and often hindering the biological purification process of the liquors, above all with reference to the high chlorides content. In particular, with reference to the BDCs, the beneficial effects of the process according to the invention can be summed up as: 1. Remarkable reduction of tne pollution load m terms of COD m the waste liquors fed to the biological treatment plant (such a load reduction is estimated to be equal to about the 15-20%), with the entailed reduction m sludge production; 2. Considerable sulphides reduction of the the waste liquors fed to the biological treatment plant, with drastic reduction of the odors emitted from the plant itself and of the sulphates the waste liquors and improvement of the sludge filtration steps 3. Remarkable chlorides reduction in the waste liquors of the biological plant (a chloπαe ion reduction of about 20-40% can be estimated) . 4. Possibility to sensibly improve the management of the biological plant itself, taking into account the lighter pollutant load and above all the aosence of compounds, present in the BDCs, that are potentially toxic to the biological plant. Even in case of treating of liquors other than the BDCs (e.g., ALPs or AFCs) benefits for the purification plant are obtained, such as a lighter chloride on concentration in the purified _ quors, and a reduced organic load, entailing a reduced sludge production.

Claims: CLAIMS 1. A process for the disposal of solid or liquid wastes deriving from treatment steps of animal origin matter, said wastes containing protein products of animal origin and products of salme nature, obtaining environmentally disposable waste liquors and recovery products useful m agriculture, livestock and industry, characterized m that it comprises, in a first stage, the steps of: hydrolyzmg said protein products in order to obtain a salme peptide liquor; purifying said peptide liquor from solids and Calcium and Sulphur compounds; and, n a second stage subsequent to said first stage, the steps of: separating the industrially useful purified sodium chloride from said peptide liquor and obtaining a treatable peptide byproduct, useful m the agricultural or livestock field or as fuel, the waste liquors having, after said two treatment stages, a residual pollutant content low enough to be deliverable to a standard purification plant, or directly to a dumping site. 2. The process according to claim 1, wherein said peptide byproduct is recovered as a dried solid, or as a peptide concentrate . 3. The process, according to claim 1 or 2, wherein said solid or liquid wastes are drained from lime pits (BDCs) . 4. The process, according to claim 1 or 2, wherein said solid or liquid wastes derive from steps related to the hide tanning field, from the concomitant BDC treatment, from salts yielded by hide beating, or from hair undissolved by tne lime bath. 5. The process according to claim 1 or 2, wherein said solid or liquid wastes derive from the processing of mammal butchery residues, fleshing or meat flours. 6. The process according to claim 1 or 2, wherein said solid or liquid wastes derive from fish or fish flour products processing. 7. The process according to any one of the preceding claims, wherein said first treatment stage comprises the steps of: accumulating said protein products of animal origin in an aqueous salme suspension; hydrolyzmg said suspension, continuously or m batches, m a markedly alkali environment with a temperature ranging from room temperature under atmospheric pressure, and 160°C under pressure in order to obtain said peptide liquor; separating the solids contained in said liquor; decalcifying said liquor reacting it with carbon dioxide or other carbonates or bicarbonates in order to produce calcium carbonate; and separating the calcium carbonate from said liquor of pH from 5 to 11, in order to obtain a limpid peptide to feed to said second stage. 8. The process according to claim 7, wherein said calcium carbonate obtained in decalcifying step is used as soil conditioner or additive m agriculture. 9. The process according to claim 7 or 8 , wherein in said decalcifying step of said liquor an acid is additioned n order to bring the pH between 5 and 8, air or Nitrogen is injected to convert the sulphides present in the solution to hydrogen sulphide and the gaseous flow is suitably treated in order to convert the hydrogen sulphide to sulphuric acid, calcium sulphate, ammonium sulphide, sodium bisulphite, sodium sulphide or sodium sulphydrate for the recovery and the reuse of said compounds . 10. The process according to claim 7 or 8, wherein after said hydrolyzmg step the alkaline suspension is acidified to a pH ranging from 0 to 6 for converting the sulphides present in the solution to hydrogen sulphide, and an oxide or earthy alkali hydroxide is added in order to precipitate the previously additioned acid as salt. 11. The process according to claim 10 wherein sulphuric acid is added in order to acidify the suspension, and calcium oxide or hydroxide in order to precipitate the calcium sulphate. 12. The process according to claim 7 or 8, wherein after the accumulation of said protein products and prior to the hydrolyzmg , the sulphides present n the solution are oxidized to thiosulphates and/or sulphates by means of a strong oxidizer, in case using a catalyst. 13. The process according to claim 7 or 8, wherein after the accumulation of said protein products and prior to the hydrolyzmg step, the salme aqueous suspension is acidified to a pH of from 3 to 6 m order to precipitate a gel of collagen proteins and to eliminate the sulphides, the solids thus obtained are separated prior to the hydrolyzmg step and are subjected to a thermal sterilization treatment to be used m the agricultural and industrial fields. 14. The process according to claim 13, wherein said sal e aqueous suspension is acidified with sulphuric acid. 15. The process, according to any one of the preceding claims, wherein said second stage comprises the steps of: concentrating said salme peptide liquor by evaporating an amount of the solution water such that a pre-concentrate wherein the salt concentration does not exceed that at the crystallization start is obtained; crystallizing the salt by further eliminating the solution water from said peptide liquor; and separating the crystallized salt from the peptide liquor in order to obtain said salt and said peptide concentrate. 16. The process, according to claim 15, wherein prior to the concentrating step, or in lieu thereof, a sal e liquor pre-concentration step is carried out by osmosis in order to increase the salt concentration m the starting liquor of from about 1.5 to 2 times. 17. The process according to claim 15 or 16, wherein said concentrating step is carried out by evaporating or cooling the solution water. 18. The process, according to any one of the claims 15 to 17, wherein said separation step of the crystallized salt from the peptide liquor is carried out by filtration or centrifugation. 19. The process, according to any one of the claims 15 to 17, wherein said peptide concentrate is subjected to a second crystallization step in order to obtain a lower salt concentration in the final peptide concentrate. 20. The process, according to any one of the claims 15 to 19, wherein said separated crystallized salt is washed with a saturated brme in order to obtain a purified sodium chloride salt. 21. The process, according to any one of the claims 15 to 20, wherein said brme is additioned with oxidizing agents m order to eliminate existing sulphide traces. 22. The process, according to any one of the claims 15 to 21, wherein said osmosis or concentration and crystallization steps can be carried out withm a single recovery step, with or without sodium chloride purification 23. The process according to any one of the preceding claims, wherein said waste liquors deriving from the evaporation and crystallization steps are purified in a purification plant comprising an ammonia stripping treatment, a treatment with oxidizing agents in order to eliminate residual sulphides, and a percolation through an active surface material.

Inventors: NERESINI MASSIMO, NERESINI, MASSIMO
Applicants: NERESINI MASSIMO, S I C IT S P A, NERESINI, MASSIMO, S.I.C.IT. S.P.A.
Application year: 2000
Main classification: C02F1
IPC codes: A23J1, A23J3, C02F1, C05D3, C05F1