TECHNICAL FIELD
The present invention relates to a separation process with
recovery of proteins and fats from substances of animal origin, organic
substances or refluent from working organic substances and a plant to carry
out the process.
BACKGROUND OF THE INVENTION
In many activity fields the need occurs of discharging organic
substances of animal origin comprising proteins and fats. This requirement
cannot be satisfied except at the cost of considerable difficulties, as
proteins and fats are polluting substances which don't allow their
immediate discharging, but on the contrary involve their preventive removal
according to the rules in force.
The present invention relates to the separation of the proteins
and fats from organic substances of animal origin which comprise them.
Furthermore as such proteins and fats are residual products having the
opportunity of being reused, the present invention also relates to their
recovery.
The fields of application of the invention are various and
concern, for example, the food manufacturing, the treatment of butchery
waste, the treatment of sewer waters; indeed a field of particular interest
is that of the leather tanning industry either for the kind of treated
substances or huge quantities involved.
As it is known the skin consists, from the chemical point of
- 2 - view, of water, fats, proteins, mineral substances, and so on. During the
tanning the skins are firstly subjected to a depilation treatment for
affecting the epidermis and the root of hairs, thus allowing their
separation from the derma, and then to a calcination treatment in which the
fats provided in the skin are saponified, the keratin forming the hairs and
the epidermis are attacked and changed into keratasis which is easily
soluble in alkaline environment, and the collagen undergoes hydrolysis
which allows it to react more easily with the tanning substances.
From the calcination treatment, which takes place in pits, the
lime pit water is obtained as a residual product which is strongly basic
and also comprising fats and proteins in non much quantity.
The depilated skins are then fleshed, that is deprived of the
adipose tissue and the calcareous residues provided in it, and then reduced
to uniform thickness. All that is obtained from this working, together with
the pieces of skin which have been discarded before the fleshing,
constitutes the "shred of flesh", a substance rich in fats and proteins.
Both the lime pit water and the shred of flesh are refuses of
the tanning industry, but they cannot be immediately discharged, as already
said, due to the high polluting substances that proteins and fats are.
For what relates to the shred of flesh, it has already proposed
to take out from this the lipidic and proteic fractions with a process
including the steps of mechanically triturating the shred of flesh, heating
it up to 50-60 °C, centrifugating it to separate a little quantity of fats
and toasting the proteic residue in a direct-heat rotary dryer.
A drawback of this known process consists in that it allows only
a partial recovery of fats, which amongs other things are of a poor
quality. Furhermore the recovered proteic fractions are denaturated as they
comprise sulfates, sulfides, chlorides and all the other chemical compounds
used in the calcination process.
Another known treatment of the shred of flesh foresees that this
is hydrolyzed by proteolysis enzymes to make easier the separation of the
fats and to allow in such a way to obtain a good lipidic fraction.
A drawback of this treatment consists in that the proteins,
which are present in the shred of flesh in a small quantity (about 10%),
are solubilized in.a large quantity of water and can be recovered only by a
quite expensive evaporation process. '
It is also known to hydrolyzed the shred of • flesh at high
temperature, but in this case a denaturation of the lipidic fraction occurs
and moreover a use of a large quantity of water.
At last it is also known to take out from the shred of flesh the
lipidic fraction by organic solvents which are later evaporated. This
process is very expensive due to the high cost of the solvent to be used
and the need of recovering the evaporated solvent which obviously cannot be
discharged into the atmosphere for polluting reasons.
For what concerns the lime pit water, a well known purification
process is based on the use of activated sludges. This process presents
- -
many difficulties of operating as the effluents coming from tanning
treatments comprise large quantity of sodium chloride and other chemical
compounds as cyanide, chlorine, cadmium and copper which reduce and at
times prevent the growth of the bacteric flora which is essential for the
purification process.
Moreover this well known purification process of the lime pit
water presents other drawbacks and i particular:
- the need of periodically stopping the plant for the evacuation of the
sludges with the consequent considerable loss of time and consumption of
energy for the subsequent restarting of the purification activity;
- the considerable energetic cost of the purification treatment;
- the need of having at disposal other purification units (usually
purifiers of an association) to treat the waters coming out from the
separate purifiers.
DISCLOSURE OF THE INVENTION
An aim of the invention is to eliminate all the above mentioned
drawbacks and to separate and recover the basic organic substances of
animal origin, proteins, fats with a process that:
- is applicable to the substances to be treated apart from their nature
and origin,
- allows to obtain with a very good efficiency a very high recovery of
proteic and fat substances,
- does not alter the recovered proteic and lipidic fractions,
- 5 -
- involves very low energetic consumptions, and
- requires a limited utilization of labour.
Another aim of the invention is to provide a plant to carry out
the process.
According to the invention these and other aims are attained
with a separation process with recovery of proteins and fats fro
substances of animal origin, organic substances or refluent from workin
organic substances including the step of:
- treating the substance with alkaline bisulfite, which reduces its p
value and partially saponifies the fats;
- adding to the so treated substance a concentrated hydroxy acid whic
disaggregates the lipidic and proteic fractions, carbonizes the presen
impurities, precipitates in an irreversible way the suspended protein
and causes the breaking of the basic soap, thus re-forming fatty aci
and partially causing an acid saponification having strong emulsifyin
properties,
- recovering with known physic techniques the most precipitated protein
and not-emulsified fats, evidentiating a watery fraction comprisin
further suspended proteins and if necessary, according to the startin
substance, an emulsified lipidic fraction which is then separated wit
known physic -techniques from the watery fraction,
- causing a pH inversion of the watery fraction thus coagulating th
suspended proteins, and
- recovering mechanically the coagulated proteins and precipitating from
the obtained watery fraction the sulfuric ions provided in it.
According to the invention to carry out the process a plant is
provided characterized in that it comprises in series:
- a first mixer for treating the first matter with alkaline bisulfite,
- a second mixer for treating the first matter, coming out from the first
mixer, with concentrated hydroxy acid,
- a separator for separating the precipitated proteins and the
not-emulsified fats from a watery fraction comprising further suspended
proteins and if necessary, according to the starting substance, an
emulsified lipidic fraction,
- a possible separator of the emulsified lipidic fraction from the watery
fraction,
- a third mixer of said watery fraction with a base to cause the pH
inversion and the consequent coagulation of the suspended proteins,
- a mechanical separator of the coagulated proteins, and
- a fourth mixer of the watery fraction, coming out from said mechanical
separator, with calcium hydroxide to cause the precipitation of the
sulfuric ions provided in it.
BRIEF DESCRIPTION OF THE DRAWINGS
The present invention is further clarified in two preferred
embodiments with reference to the enclosed drawings.
Figure 1 shows schematically a plant to carry out the process according to
- - the invention,
Figure 2 shows a block diagram illustrating the various step of the
process, and
Figure 3 shows schematically a plant to carry out the process in a second
5 embodiment.
BEST MODE OF CARRYING OUT THE INVENTION
As it can be seen from the drawings the plant ' to carry out the
process according to the invention comprises a screw mixer 1 to which a
displacement pump 2 is connected introducing sodium bisulfite. The outlet
10 of the mixer 1 is connected to a mixer 3, to which a displacement pump 4 is
connected introducing concentrated sulfuric acid. At the outlet of the
mixer 3 an agitator 5 is provided to which two vessels 6 and 7 are
connected comprising respectively sulfuric acid and caustic soda.
The outlet of the agitator 5 is connected to a continuous press
15 8, in its turn connected to a static decanter 9. At the outlet of the
decanter 9 a three-way valve 10 is provided having one outlet connected to
a mixer 11 and the other outlet connected to a filter 12 in its turn
connected to a plate centrifugal separator 13. The oulet of the centrifugal
separator 13 is connected, as well as the first outlet of the valve 10, to
20 the mixer 11 to which also a vessel 14 of caustic soda is connected.
The outlet of the mixer 11 is connected by choice, through a
three-way valve 19 to a filter press 17 or to a continuous press 18, having
their outlets of the watery fraction connected to a mixer 15, to which the
- 8 - outlet of a vessel 16 of calcium hydroxide 16 is connected.
The outlet of the mixer 15 is connected by choice, through a
three-way valve 20, to the outside of the plant for the disposal or to the
mixer 1 for the recycling.
The operating of the described plant carrying out the process
according to the invention is the following:
the treated first matter, which in the case of the tanning industry can be
shred of the flesh or the lime pit water, is introduced into the screw
mixer 1. In the case of the shred of flesh, it is subjected to a
trituration pre-treatment.
While the first matter is introduced into the mixer 1, it is
sprayed with sodium bisulfite causing the partial saponification of fats
and the pH reduction. The so treated first matter is transferred into the
mixer 3 where to it concentrated sulfuric acid is added making easier the
breaking of the membranes keeping the fats and causing the irreversible
precipitation of the proteins which are in solution or hydrolyzed.
More particularly the concentrated sulfuric acid acts on the
glycerides of the not-saturated acids, adding itself to their double bonds
and forming an unstable saturated glyceride, the tristearinsulfonic, which
is converted into glycerin and sulfostearic acid having high emulsifying
properties; the glyceride allows the scission of the fats in presence of
water.
Therefore in the mixer 3, other than the precipitation of the
- - fibrous proteins, the complete saponification of the fats, which have no
been saponified in the mixer 1, the breaking of the basic soap and th
re-formation of the fatty acid occur.
As the first matter introduced into the mixer 1 can hav
different characteristics also changeable with the passing of the time, i
is foreseen that at the outlet of the screw mixer 3 a pH control occurs
and if necessary a correction in the agitator .5 by introducing a correc
quantity of caustic soda or sulfuric acid to cause the optimum condition
of acidity of the first matter.
The first matter is then introduced into the continuous press
in which the separation of thefibrous proteins occurs from the watery
fraction comprising fats and suspended proteins and which is introduce
into the decanter 9.
There the separation of the not-emulsified fats occurs (whic
come up to the surface and can be forwarded to a collection place of th
fats) from a proteic sand (sedimenting on the bottom and wich can b
forwarded together with the fibrous proteins coming out from the continuou
press 8 to a collection place of the proteins) and from a watery fraction.
The composition of this watery fraction will be differen
according to the kind of the first matter.
If the first matter is lime pit water, the watery fraction onl
comprises suspended proteins whereas if the first matter is shred of flesh
the watery fraction also comprises emulsified fats other than proteins. I
- 10 - the first case it comes out from the valve 10 and directly reaches the
mixer 11, whereas in the second case it comes out from the valve 10,
reaches the filter 12, where the separation of the small mineral and
organic impurities and in case of emulsified fats occurs, and then the
centrifugal separator 13, where the separation of the fats from te watery
fraction comprising the suspended proteins occurs. Then the fats are
forwarded, together with those coming out from the decanter 9 to the
suitable collection place while the watery fraction is introduced into the
mixer 11. Here to the watery fraction, both coming out directly from the
decanter 9 and from the centrifugal separator 13, caustic soda is added
causing a sudden pH inversion and a consequent coagulation of the suspended
proteins. According to the sizes of the proteic particles, the watery
fraction passes from here, through the three-way valve 19, to the filter
press 17 or continuous press 18. Here the separation of the proteins occurs
which are collected together with those previously separated from the
watery fraction which is introduced into the mixer 15 and to which calcium
hydroxide is added to let the precipitation of the present sulfuric ions
take place.
The water coming out from the mixer 15, being in practice
lacking in polluting substances, can be directly discharged upon a possible
neutralization and desalination, this latter in order to allow the recovery
of the salts, or can be reused for further treatments also in the same
tannery, or, if the further extraction of the proteins is required,
- - reintroduced into the mixer 1 for the repetition of the cycle.
The process according to the invention and the plant to carry
out it allow to recover from the polluting first matter a lipidic fraction
which advantageously can be used for the alimentation in zootechnical
5 field, for the manufacturing of oils and soaps in cosmetic field and in
general in the stearic industry; a proteic fraction which in the same way
can advantageously be used in zootechnical and fishing field as fertilizer
and corrective; and a watery fraction which can be discharged without any
polluting hazard or can be reused, as already said, in the same tannery
10 both for repeating the calcination or washing phase on other skins, and for
diluting refluent waters which in themselves have polluting substances
higher than those the rules allow and therefore could not be directly
_ discharged.
Always in the tanning industry the process according to the
15 invention is very advantageous boh with respect to the traditional process
of treatment of the shred of flesh and to the traditional treatments of
lime pit water.
For what relates to the treatment of the shred of flesh, the
process according to the invention can be carried out cold and therefore
20 requiring a low consumtion of energy, not damaging the proteic substances
and the recovered fats, is extremely quick and requires low fixed assets.
For what relates to the treatment of lime pit water, the process
according to the invention
- 12 -
- requires energetic consumption so low as it cannot compared with thos
of the purifiers used at present,
- is of complete reliability not depending upon the growth of bacteri
flora which feels the affects of several factors such as the pH of th
first matter, the composition of the nutritional substratum, th
temperature and the seasonal conditions,
- allows to eliminate a possible source of poisonous gases formed by th
conversion of the sulfide into sulfydric acid, and
- allows to obtain commercial products having a value higher than th
treatment cost.
The following example serves to further clarify the invention:
in the mixer 1 to 1178 Kg of triturated shred of flesh subjected to a
expression pretreatment for eliminating some water 8.8 Kg of sodiu
bisulfite have been added and the whole has been transferred into the mixe
3, where 89 Kg of concentrated sulfuric acid at 98% have been introduced.
The product at the outlet of the mixer 3 had pH 2. Then it has bee
transferred into the continuous press 8 without the need of any p
correction and here the separation of 551 Kg of fibrous proteins having
humidity of 42.83%, a specific weight of 1.129 Kg/dm3 and a content of fa
matter of 6.77% occurred.
The watery fraction coming out from the continuous press 8 ha
been forwarded to the filter 12 and subsequently to the centrifuga
separator 13, where 15 Kg of emulsion, fat at 96.67%, having a humidity o
- - 3% and 0.09% of free glycerin. The composition of the separated fats in the
centrifugal separator 13, of which 7.6% consisted of glyceryn, resulted the
following:
capric acid 0.1%
lauric acid 0.15%
myristic acid 4.1%
C- 14 1.95%
n-pentadecanoic acid 0.4%
palmitic acid 30%
palmitoleic acid 7.7%
n-heptadecanoic acid 1%
C- 17 1%
stearic acid 9%
oleic acid 41.5%
linoleic acid 1.74%
eicosanoic acid 0.21%
linolenic acid 0.6%
The watery fraction separated in the centrifugal separator 13
consisted of 628 Kg of refluent water comprising 2.6% of soluble sodium
sulfate and 2.9% of proteins. This watery fraction has been introduced into
the agitator 11 and here to it an aqueous solution comprising 300 g of
NaOH has been added, causing the coagulation of 18 Kg of humid proteins to
be forwarded to the filter press 17 or the continuous press 18.
- 14 - The water treated with caustic soda has been introduced into th
agitator 15 where to it an aqueous solution comprising 300 g of calciu
hydroxide has been added which caused the precipitation of about 8 Kg o
insoluble calcium sulfate.
In the embodiment schematically shown in Figure 3, the outlet o
the filter 12 is connected to a set of receivers, indicated with th
reference number 21, having the function of natural decanters, and the
have the upper outlet connected to the centrifugal separator 13, the middl
outlet connected to the mixer 11 and the bottom outlet connected to th
collection place of proteins. The outlet of the centrifugal separator 13 i
connected to the set of receivers 21.
The operating of the plant according to this second embodimen
is the following:
the watery fraction coming out from the filter 12 is introduced into th
receivers 21 where a natural decantation slowly occurs separating a fa
fraction (on the upper part) which is forwarded to the centrifuga
separator 13, a watery fraction (on the middle part) comprising suspende
proteins which is forwarded to the mixer 11 and a proteic sludge (on th
lower part) forwarded to the collection place of proteins.
The watery fraction coming out from the centrifugal separator 1
is reintroduced into the receivers 21 to allow a further separation of th
fats, which inevitably are present in it.
This second embodiment offers, with respect to the previous one
- 15 - the possibility of separating from the watery fraction coming out from the
filter 12 a fraction richer in fats and a proteic sludge which can be
directly forwarded to the collection place of the fats and to the
collection place of proteins, increasing in such a way the efficiency of
the centrifugal separator 13 and allowing at the same time a direct
recovery of the proteic sludges which theyselves are a product that can be
directly used, particularly in the fodder field.