WO2021066664A1

WO2021066664A1 - Process and facility for the production of charcoal and pyroligneous liquids from woody or herbaceous vegetal material

Info

Publication number: WO2021066664A1
Application number: PCT/PT2019/000007
Authority: WO
Inventors: Pedro Luis DE ALMEIDA FERREIRINHA
Original assignee: Bgw, S.A.
Priority date: 2019-10-03
Filing date: 2019-10-03
Publication date: 2021-04-08

Abstract

The invention relates to a process and facility for producing charcoal and pyroligneous liquids from woody or herbaceous vegetal material, comprising the steps of: homogenization of the raw material (biomass B); drying of the biomass (B) in the drying oven (2); loading of the biomass into a cylindrical and removable container (3.1); introduction of a cylindrical and removable container (3.1) into the furnace (3.2) of the pyrolysis reactor (3); pyrolysis of the biomass (B); condensation of the condensable gases and vapours leaving the pyrolysis reactor (3); removal of the removable cylindrical container (3.1) from the furnace (3.2) and discharge of the charcoal from the inside of the removable cylindrical container (3.1); washing of the non-condensable gases; decantation of the pyroligneous liquids; wherein the process further comprises the steps of: partial recirculation of the pyroligneous liquids from the pyroligneous condensation liquid collecting reservoirs (L1), by a recirculation pump (12), via a recirculation loop (LA) which feeds flush nozzles (13) in ducts; constant flushing of these ducts (3C and 3G), to prevent them from becoming obstructed by vegetal tar deposits present in the pyrolysis vapours and gases, the pyroligneous liquids used to flush the ducts being drained and dragging therewith the condensable tar vapours, passing subsequently through the condensers (G1) where they are cooled before returning to the condensate collecting reservoir; and the decantation of the aqueous fraction of the pyroligneous liquids in the low temperature decanter (L3) thermally insulated with refrigeration loops where a residence period is carried out with an average duration of 8 hours at a temperature of 5,5°C ± 2,5°C, with the precipitation of the light tars, which, after passing through a charcoal filter (47), allows tar contents lower than 0.2% to be obtained in the outlet, after said residence period of the aqueous fraction of the pyroligneous liquids. The invention also relates to installation A for carrying out the above-mentioned process.

Description

DESCRIPTION

“Process and installation for the production of charcoal and pyroligneous liquids from woody or herbaceous plant material”

Field of invention

[0001] The present invention relates to a process and installation for the production of charcoal and pyroligneous liquids.

Previous art

[0002] The phrase “woody and herbaceous plant material”, used herein and hereinafter referred to as biomass, broadly includes biomass, such as wood, logs, branches, sawdust, etc. This term is also intended to include processed cellulosic materials, such as cellulose, cardboard, paper, bagasse, rope and other biomass of vegetable origin.

[0003] In accordance with the present invention, woody or herbaceous plant material (biomass) is converted to charcoal by pyrolytic conversion.

[0004] The production of charcoal has been a practice known for a long time in the history of mankind, and references to its production have existed for several centuries. However, the great evolution of industrial charcoal production techniques occurred during the course of ^the Second World War, in which the objectives were multiple, such as the supply of raw material for industry, the production of coal for gasifiers, the synthesis of fuels, etc.

[0005] The term pyrolysis is used to characterize the thermal decomposition of carbon-containing materials, in the absence of oxygen.

[0006] Carbonization results from the heating, at temperatures between 300 ° C and 600 ° C, of a raw material in an oxygen-free environment, in this case of biomass, until its partial decomposition.

[0007] The result of this thermochemical treatment is to obtain three fractions in different phases of matter, a fraction consisting of solid products, charcoal, another fraction consisting of liquid products, derived from condensable volatile products, and yet a another fraction consisting of non-condensable volatile products, ie gases from biomass. [0008] Two equivalent terms are usually applied to the same chemical process: “carbonization” when aiming to obtain charcoal as the most important product or “dry distillation” if the recovery of chemicals represents an important economic factor.

[0009] There are basically two known processes for carbonizing wood. The first is the oldest which, over the centuries, has undergone changes in its shape and ability to improve its performance. It is called “Partial Combustion Process”. As the name implies, it is a process in which part of the biomass is burned, with the aim of producing heat to heat and carbonize another part of the biomass,

[0010] The second process, of more recent origin, diversified in the 19th century, because the number of devices is due to the use of the by-products of distillation; it is called "Process of heating by external heat source" or, simply put, "Process without combustion".

[0011] In this process, heating is usually done using hot gases, as a heat carrier, and which can be called internals when they cross the bed of biomass to be carbonized and externals when they do not come into contact with the same. This system, when equipped with suitable devices, in addition to carbonizing with great yield, allows the use of by-products.

[0012] The theory of biomass distillation is well known and it has not changed in its fundamental principle. The innovations introduced in the processes refer almost entirely to the devices used. A typical distillation consists of a container with external heating, where 200 ° C will produce almost exclusively water vapor (drying period). In the range of 270 ° C to 380 ° C, the pyrolysis reaction takes place, which is exothermic and is characterized by the strong release of volatiles, mostly acetic acid, methyl alcohol and light tar fractions, as well as combustible gases. In the range of 380 ° C and 600 ° C, as the temperature increases, large volumes of gases will decrease, with products composed mainly of medium and heavy tar fractions now being released.

[0013] The liquid products from the condensation of the volatile gases released are made up mostly of water (70% to 85% of all condensable products), followed by acetic acid, methyl alcohol, acetone and tars.

[0014] Normally condensable products are separated by resting in three layers: a lower layer formed by crude tar, an aqueous intermediate layer, where acetic acid, methyl alcohol, acetone and dissolved soluble tars are found, and a thin top layer of light oils. The middle layer is called acid or pyroligneous liquid. The rest period that precedes the decantation process to separate the layers mentioned is generally between 6 to 18 months, depending on the technical and lighting conditions to which the layers are subjected.

Object of the invention

[0015] The invention has as its object a process and installation for the production of charcoal and pyroligneous liquids from woody or herbaceous plant material, by means of which the biomass is subjected to a pyrolysis by heating in a pyrolysis reactor, which comprises a removable container, obtaining coal that remains inside said removable container for a substantially shorter period of time than in the prior art devices, which period should be less than six hours.

[0016] The fact that the pyrolysis reaction is carried out in a removable container translates into a benefit in terms of the production of said coal and by-products, since the possibility of being able to introduce and remove said removable container from the remaining part of the pyrolysis reactor allows a continuous production of the installation composed of several associated pyrolysis reactors, preferably in number of four or more. While the coal is being discharged from a removable container in a pyrolysis reactor and cleaning and maintenance operations are being carried out on the removable container, the other pyrolysis reactors remain in coordinated operation, in such a way that the installation produces continuously, as it is always at least one other pyrolysis reactor in operation.

[0017] The purpose of the invention is thus the continuous production of coal and by-products of good quality with coordinated maintenance operations of the devices, increasing the overall performance of the installation compared to known installations.

Summary of the invention

[0018] The present invention provides a simpler, more efficient and faster process of producing charcoal with the use of condensable and non-condensable vapors from the biomass pyrolysis process. This invention allows the continuous flow separation of the pyrolytic liquids in the organic and aqueous fractions, without needing to subject the pyrolytic liquids to long periods of rest for months, for later separation.

[0019] This process allows a better ratio of coal production per unit of biomass used, a reduction in the storage time and drying of the biomass and a reduction in the cooling time of the coal, obtaining a product with characteristics of better regularity and uniformity without harmful gas emissions to the atmosphere.

[0020] It is an improved batch process for each pyrolysis reactor where the pyrolytic conversion of biomass into charcoal is carried out, which was transformed into the installation by combining several pyrolysis reactors in a continuous process. The charcoal produced has a fixed carbon content, but it is adjustable, which allows to achieve yields that vary from 30 to 40% based on dry weight, depending on the material and the desired fixed carbon content.

[0021] This discontinuous production process for each of the pyrolysis reactors must be carried out in at least 6 hours or more for each pyrolysis reactor, the respective recharge with biomass being practically instantaneous without substantial cooling of the pyrolysis reactor and without expose the processed hot coal to air or oxygen, which may cause the coal to burn after removal of the pyrolysis reactor.

[0022] Each pyrolysis reactor is equipped with a burner that can operate with pellets or other fuel for the start-up. After start-up, with the use of at least four pyrolysis reactors operating in a coordinated manner, that is to say, lagged, it is possible to obtain continuous combustible gases that energize the pyrolysis reactors.

[0023] The hot gases, produced by combustion in the furnace of each pyrolysis reactor, are used to feed the drying oven that dries the biomass before it is loaded in each pyrolysis reactor, more specifically in the removable container.

[0024] The fact that the biomass is loaded in the removable container with low moisture and hot content, and the removable container being introduced in the pyrolysis reactor, coupled with the fact that the pyrolysis reactor is hot (due to the fact that it is not necessary to cool to make the removal and reintroduction of the removable container) allows for high energy efficiency and, consequently, also reduces the cycle time of the process, thus making the process overall more efficient.

[0025] This invention solves two problems that, sometimes, make projects economically unfeasible and that occur when the use of pyrolytic liquids is made, which are: the clogging with the tar that is deposited on the walls of the ducts covered by vapors and gases that come out of the pyrolysis reactors; and the enormous liquid storage needs, associated with the rest time necessary for the stratification of liquids for subsequent separation by decantation.

[0026] The problem of clogging the ducts is overcome through a system for washing the ducts of vapors and gases by using a recirculation circuit with dispersers that inject pyrolytic liquid at the critical points of the system.

[0027] The problem associated with the huge volumes of storage necessary for the liquid's rest period is solved through the system of successive decantations with filtration.

Brief description of the drawings

[0028] The characteristics of the present invention will become evident in the description of the currently preferred embodiment, given as a non-limiting example of the invention and with reference to the accompanying drawings, in which: Fig. 1 is a schematic diagram of the operation overall process of the present invention; Fig. 2 is a schematic view of the installation for the production and treatment of pyrolysis products; Figs. 3a and 3b are, respectively, a sectional view of the pyrolysis reactor (furnace and container set) and a sectional view of the pyrolysis reactor furnace; Figs. 4a, 4b and 4c are respectively top, side and side views in section of the cylindrical and removable container of the pyrolysis reactor; Fig. 5 is a cross-sectional view of the condenser; Fig. 6 is a sectional view of the washer of non-condensable gases; and Fig. 7 is a sectional view of the low temperature decanter.

Detailed description of the invention

[0029] The process of producing charcoal and pyroligneous liquids from woody or herbaceous plant material of the present invention will be described hereinafter together with the schematic diagram shown in Fig. 1 and the schematic of the installation of production and treatment of the pyrolysis products shown in Fig. 2, in which only one reactor is represented, however this installation includes four reactors, the devices being both upstream and downstream of the represented reactor common to the four reactors.

[0030] Referring to Figs. 1 and 2, the raw material used in the process of the present invention can have any convenient shape, ranging from small pieces to logs with 100 millimeters or more in diameter and up to several meters in length, with moisture contents that can vary from 5 % up to 50% of its weight on a wet basis.

[0031] The process of producing charcoal and pyroligneous liquids from woody or herbaceous plant material comprises the steps of: homogenization of the raw material (biomass B), carried out in a cutting / fragmentation device 1, where it is cut and / or fragmented to obtain the desired dimensional homogenization (for example 80mm) to be fed to the drying oven 2; drying, carried out in drying oven 2, of biomass B, dimensionally homogenized, in which a mixture of hot combustion gases and air 2C is insufflated, with hot gases 2A coming from the pyrolysis reactor furnace and air 2B limiting the temperature of hot combustion gases. In this drying step, biomass B remains inside drying oven 2 for a period necessary to obtain a sufficient degree of humidity, for example, greater than 10%; the mixture of hot combustion gases and air 2C circulates inside the drying oven 2 in a turbulent environment, crossing the biomass bed B until the exit at the opposite end of the drying oven 2, through a 2D chimney, dragging with it the moisture present in biomass B and also causing the heating of biomass B to a temperature, for example, greater than 90 ° C; loading of biomass B, after reaching the desired humidity level, for example less than 10%, in the drying oven 2, into a removable 3.1 cylindrical container, which is then hermetically closed; biomass B, loaded in the removable 3.1 cylindrical container, has, in this step, a reduced moisture content, for example, less than 10% and is heated to a temperature, for example, greater than 90 ° C, which allows a reduction in the time required for pyrolysis; introduction of a removable cylindrical container 3.1 inside the furnace 3.2 of the pyrolysis reactor 3; pyrolysis, initiated at an elevated temperature, greater than 260 ° C, in this step the biomass B is subjected to pressures between 200 Pa and 1000 Pa and at a temperature between 400 ° C and 550 ° C; the exact residence time of biomass B inside the cylindrical and removable container 3.1 of the pyrolysis reactor 3 will depend on the type of biomass B used, its dimensions and its moisture content, but the residence time must be less than six hours (6h); the optimal conditions for carrying out the pyrolysis step of a given biomass B can be readily determined by a person skilled in the art by carrying out tests with samples of the particular biomass B; condensation of vapors and condensable gases, which leave the pyrolysis reactor 3 through conduit 3C and which are routed through conduit 3G to condenser G1, the resulting condensed liquids being collected in the collection reservoirs for condensation pyrolytic liquids L1 and the gases being non-condensables sent to the G2 gas scrubber; removing the removable cylindrical container 3.1 from the furnace 3.2 with the coal in it after finishing the pyrolysis step without having to cool the pyrolysis reactor 3 and unloading the coal from inside the removable cylindrical container 3.1 after the coal has cooled to lower temperatures than 60 ° C; washing of non-condensable gases, performed in the G2 gas scrubber, which are sent to the combustion chambers (furnaces) of the pyrolysis reactors 3, where they are burned and generate the heat necessary for the biomass B pyrolysis process; whenever necessary, the pressure in the non-condensable gas circuit is relieved, by using a discharge valve (not shown) that releases the gases through a torch 3B, which guarantees the burning of these gases, minimizing atmospheric emissions: partial recirculation of the pyrolytic liquids from the L1 condensation pyrolytic liquid collection reservoirs by a recirculation pump 12, through a LA recirculation circuit that feeds washing dispersers 13 in the 3C and 3G conduits; constant washing of these 3C and 3G ducts, to prevent them from being obstructed by depositions of vegetable tar present in the vapors and pyrolysis gases, the pyrolysis liquids being used to wash the ducts, drained and dragging with them the condensable tar vapors, then passing through the capacitors G1 where they are cooled before returning to the condensate collection tank L1; decantation of pyro-wood liquids in the L1 condensation pyrolytic liquid collection reservoirs, which are sent to L2 decantation columns, which promote the separation of heavy tars from the aqueous fraction which at this stage still contain a high content of light tars which may be higher to 3%; decantation of the aqueous fraction of pyroligneous liquids in the L3 low temperature decanter, thermally insulated with refrigeration circuits where an average duration of 8 hours is maintained at a temperature of 5.5 ° C ± 2.5 ° C, with precipitation of the light tars, which after passing through a charcoal filter, allow to obtain at the outlet, after the time of permanence of the aqueous fraction of the pyroligneous liquids, tar contents of less than 0.2%.

[0032] Plant A for the production of charcoal and pyroligneous liquids from woody or herbaceous plant material comprises at least one biomass B cutting / fragmenting device 1, at least one drying rape 2, fed by, at least one mixer of hot combustion gases 2A and air 2B, at least four pyrolysis reactors 3, each pyrolysis reactor 3 being equipped with a cylindrical and removable container 3.1, 3C and 3G ducts for vapors and gases of pyrolysis, using a redrculation circuit with duct washing dispersers 13, which inject pyroligneous liquid at the critical points of the system, a G1 condenser, a fan 15 that circulates the non-condensable gases that move into the gas washer G2, a collection tank for the collection of pyroligneous condensation liquids L1 connected to a recirculation circuit LA that passes through a recirculation pump 12, a decanter L2, a decanter of low te temperature L3, a tar reservoir 20, a reservoir of pyrolytic acid 19 and a reservoir of light oils 18. Said installation A further comprises a pre-cooling zone S1, a hopper S2 for unloading coal and a tunnel with a system for cooling and drying 53 of the coal as well as a mechanical screen S4 for separating the coal in the desired dimensions SA1 and SA2.

[0033] The biomass B cutting / fragmenting device 1 allows to cut, fragment and dimensionally homogenize biomass B to the desired size.

[0034] Drying oven 2 dries biomass B by insufflating a mixture of hot combustion gases and 2C air, carried out in a turbulent manner, with the hot gases coming from furnace 3.2 of the pyrolysis reactor 3, destined to the air 2B limits it · the insufflation temperature of the hot combustion gases in the drying oven 2, crossing the mixture of hot combustion gases and air 2C through the biomass bed B and dragging with it the moisture present in the biomass B. [0035] Hot biomass B with low moisture content is loaded into the cylindrical and removable container 3.1, which is watertight, and introduced into the furnace 3.2 of the hot pyrolysis reactor 3 (due to the fact that it is not necessary to cool it for remove and insert the cylindrical and removable container 3.1), which allows for high energy efficiency and, consequently, allows to reduce the cycle time of the process, thus making the installation work more efficiently.

[0036] The cylindrical and removable container 3.1 is removed from the furnace 3.2 with the coal inside it after finishing the pyrolysis step without having to cool the pyrolysis reactor 3 (furnace assembly 3.2 plus cylindrical container 3.1) and being introduced a another cylindrical and removable container 3.1 filled with biomass B without cooling Significant from furnace 3.2 of the pyrolysis reactor 3.

[0037] The cylindrical and removable container 3.1 is moved to a pre-cooling zone S1 in which, after a certain period at room temperature, the coal cools to temperatures below 60 ° C.

[0038] The coal from the said cylindrical and removable container 3.1 is unloaded in an S2 hopper that has water dispersers (not shown) that humidify the coal to mitigate the risk of fire.

[0039] The wet coal in the hopper S2 is sent to a cooling and drying tunnel S3 which, when drying the coal, finishes cooling it through ventilation and through evaporative cooling.

[0040] The coal at the exit of this drying tunnel S3 passes through a mechanical screen S4 that separates the coal by size in the desired gauges SAI, SA2, etc., then the different gauges of coal are sent to packaging devices,

[0041] The 3C and 3G ducts constitute a recirculation circuit with dispersers 13 that inject pyroligneous liquid at the critical points of the system to prevent tar clogging in the said 3C and 3G ducts.

[0042] The L3 low temperature decanter operates at a temperature of 5.5 ° C ± 2.5 ° C and decants with filtration, which allows the resolution of the problem associated with the huge storage volumes for the liquid decanting phase. .

[0043] Non-condensable gases can be used in an external burner to generate heat for other processes or they can be used to activate motor-generator sets (not shown) for the production of electrical energy. [0044] During the start-up of the installation and / or on time, it is possible to verify the need for an external source of energy in each pyrolysis reactor 3 to safeguard the desired process temperatures ^; , for this purpose pellet burners or other available fuel may be used.

[0045] A suitable sensor (not shown) is used, which can be a pressure transducer or other, capable of measuring the level of precipitated tar, and the level control is carried out by sending this tar to the tar reservoir 20.

[0046] This way it is possible to separate the organic and aqueous fractions in a continuous way, avoiding long periods of rest in cool environments and protected from light to occur stratification and subsequent separation.

[0047] The cylindrical and removable container 3.1 is hermetically closed, it has only one outlet of vapors and pyrolysis gases 3C with a device that allows the release of vapors and gases released by biomass B, but does not allow air to enter from the outside.

[0048] An important feature of the present invention is that it is possible to remove the cylindrical and removable container 3.1 with the coal from the remaining part 3.2 (furnace) of the pyrolysis reactor 3 after the pyrolysis process is finished without having to cool it down.

[0049] Immediately after removing the cylindrical and removable container 3.1 filled with hot coal from furnace 3.2 of the pyrolysis reactor 3, another cylindrical and removable container 3.1 filled with biomass can be introduced into the pyrolysis reactor 3 and heated again without being No significant cooling of furnace 3.2 of the pyrolysis reactor 3 is required.

[0050] The 3C piping connected to the cylindrical and removable container 3.1 is closed with the aid of a plug, which prevents the entry of air into the cylindrical and removable container 3.1 and, thus, the hot coal inside the non-removable and cylindrical container can burn.

[0051] This cylindrical and removable container 3.1 is moved to a pre-cooling zone SI in which, after a certain period at room temperature, the carbon cooled to temperatures below 60 ° C is discharged from the cylindrical and removable container 3.1 in a hopper. S2 that has water dispersers (not shown) that wet the coal.

[0052] The wet coal in the hopper S2 is sent to a drying tunnel S3 which, when drying the coal, finishes cooling it through ventilation and by evaporative cooling. [0053] The coal at the exit of this drying tunnel S3 passes through a mechanical screen S4 that separates the coal by dimension in the desired gauges (SA1, SA2, etc ...), and is then sent to packaging devices.

[0054] Still with reference to Fig.2, a fan 15 that acts on non-condensable gases (CNG) that move into the G2 gas washer can be perceived. Installation A is equipped with a low temperature decanter L3 from where the tar passes to the tar reservoir 20 and the pyroligneous acid passes to the pyroligneous acid reservoir 19. The light oils that accumulate in the low temperature decanter L3 are discharged for the light oil tank 18.

[0055] Referring to Fig. 3a and 3b of the drawings, the pyrolysis reactor 3 comprises a removable cylindrical container 3.1 and a furnace 3.2 which comprises a refractory brick lining 23. The supports 30 serve to support the flange which in turn instead it supports the cylindrical and removable container 3.1 in the pyrolysis reactor 3 and in the qiial biomass B is loaded and from which the coal is discharged after the pyrolysis reaction.

[0056] Between the refractory brick cladding 23 and the outer side wall there is a thermal insulation 22. A chimney 28 is arranged in the furnace 3.2 which allows the exhaust gases from the pyrolysis reactor 3 to be exhausted.

[0057] In the upper part of the furnace 3.2 of the said pyrolysis reactor 3 there is a flange that contains seals before 21 qtie perform the sealing between the furnace 3.2 and the cylindrical and removable container 3.1

[0058] The pyrolysis reactor 3 of Fig. 3a and 3b further includes a gas supply 25, an air supply 26 and a burner 27 disposed in the lower outer part of said pyrolysis reactor 3,

[0059] Referring to Figs. 4a, 4b and 4C of the drawings, the cylindrical and removable container 3.1 consists of a lid 34 which is fastened by means of the seals 21 on the upper structure of the pyrolysis container by means of screw-nut tightening 35 and which seals said container cylindrical and removable 3.1. In the center of the said lid, a part of piping 3C comes out with a conical coupling 29, which is equipped with a device that allows the escape of vapors but prevents the entry of air into the cylindrical and removable container 3.1.

[0060] Referring to Fig. 5 of the drawings, the structure of the condenser G1 has an inlet of pyrolapid vapors 36 with a plurality of pipes for the passage of pyrolapid vapors 40. The condenser includes a coolant inlet 41 and a coolant outlet 38. There is also a non-condensable gas outlet 37 in the structure and an outlet for condensed liquids 3H.

[0061] Referring to Fig. 6 of the drawings, the structure of the G2 gas scrubber has a non-condensable gas inlet 16 and a non-condensable gas outlet 17. The said structure also includes a pyrolytic liquid inlet 39 and means of level regulation (not shown). Said gas scrubber G2 also includes a pyroligneous liquid outlet 40a and a drain 49 to leak in case of maintenance.

[0062] Referring to Fig. 7, said low temperature decanter L3 includes inside a coil of the cooling circuit 42 and a carbon filter 47. The structure of said low temperature decanter L3 comprises an inlet of pyrolytic liquid 43, a light oil outlet 44, a pyrolytic acid outlet 45 as well as a tar outlet 46. Said structure of the low temperature decanter L3 further comprises thermal insulation 48.

[0063] The following is a table showing the utilization rate that can be obtained with an installation according to the invention.

Table 1 - Production ratios, eucalyptus wood, coal with 90% CF content

List of alphanumeric references

[0064]

The Installation

G1 Condenser

G2 Gas washer

L1 Collection tanks for pyrolytic condensation liquids

L2 Decanting column

L3 Low temperature decanter

LA Recirculation circuit

B Biomass 51 Pre-cooling zone

52 Hopper

53 Drying tunnel

54 Mechanical screen

SA1 and SA2 Coal dimensions

1 Cutting / fragmenting device

2 Drying stove

2 A Hot combustion gases

2B Air inlet

2C Mixture of hot combustion gases and 2D air Chimney

3 Pyrolysis reactor

3.1 Cylindrical and removable container

3.2 Remaining part of the pyrolysis reactor 3 (furnace)

3B Torch

3C Conduct

3G Conduct of vapors and pyrolysis gases if

3H Condensed liquid outlet

12 Recirculation pump

13 Pipeline washing dispersers

15 Fan

16 Intake of non-condensable gases

17 Output of non-condensable gases

18 Light oil reservoir

19 Pyrolenous acid reservoir

20 Tar reservoir

21 Vedanles

22 thermal insulation

23 Refractory brick cladding

25 Gas supply

26 Air supply

27 Burner

28 Chimney

29 Conical coupling

30 Support

34 Tampa

35 Means for tightening the screw-nut

36 Intake of pirolenhos vapors

37 Output of non-condensable gases

38 Coolant outlet

39 Pyroligneous liquid inlet 40 Pyroligneous vapor passage tubes 40a Pyroligneous liquid outlet

41 Coolant inlet

42 Cooling circuit

43 Pyroligneous liquid inflow

44 Leaking light oils

45 Pyrolenous acid outlet

46 Tar exit

47 Carbon filter

48 Thermal insulation

49 Drain

Claims

1 - Process of production of charcoal and pyroligneous liquids from woody or herbaceous plant material that comprises the steps of: homogenization of the raw material (biomass (B)), carried out in a cutting / fragmentation device (1), where the it is cut and / or fragmented to obtain the desired dimensional homogenization (for example 80mm) to be fed to the drying oven (2); drying, carried out in the Drying oven (2), of biomass (B), dimensionally homogenized, in which a mixture of hot combustion gases and air (2C) is blown, with the hot gases (2A) coming from the furnace (3.2) of the pyrolysis reactor (3), and with the air (2B) to limit the temperature of the hot combustion gases, remaining in the biomass (B) inside the drying oven (2), for a period necessary to obtain a degree of humidity less than 10% and a temperature greater than 90 °; loading the biomass (B) into a cylindrical and removable container (3.1), which is then hermetically closed; introduction of a cylindrical and removable container (3.1) inside the furnace (3.2) of the pyrolysis reactor (3); pyrolysis, initiated at an elevated temperature, greater than 260 ° C, in this step the biomass (B) is subjected to pressures between 200 Pa and 1000 Pa and at a temperature between 400 ° C and 550 ° C, remaining the biomass ( B) inside the cylindrical and removable container (3.1) of the pyrolysis reactor (3) for less than six hours

(6h); condensation of condensable vapors and gases, which leave the pyrolysis reactor (3) through the conduit (3C) and which are routed through the conduit (3G) to the condenser ((31), the condensation liquids being collected in the collection reservoirs of condensation pyrolytic liquids (L1) and the non-condensable gases being sent to the gas washer (G2); removal of the removable cylindrical container (3.1) from the furnace (3.2) with the coal in it after the pyrolysis step has ended without having to cool the pyrolysis reactor (3) and discharge the coal from the removable cylindrical container (3.1) after the coal has cooled to temperatures below 60 ° C; washing, of non-condensable gases, carried out in the gas washer (G2), which are sent to the combustion chambers (furnaces) of the pyrolysis reactors 3, where they are burned and generate the heat necessary for the biomass pyrolysis process

(B); decantation of pyrolytic liquids in the collection tanks for pyrolytic condensation liquids (LI), which are sent to decantation columns (L2), which promote the separation of heavy tars from the aqueous fraction, which at this stage still contain a high content of light tars; the process being characterized by still comprising the steps of: partial recirculation of the pyrolytic liquids, coming from the collection tanks of pyrolytic condensation liquids (11), by a recirculation pump (12), through a recirculation circuit (LA) that feeds washing dispersers (13) in the ducts (3C and 3G); constant washing of these ducts (3C and 3G), to prevent them from being obstructed by depositions of vegetable tar present in the vapors and pyrolysis gases, the pyrolysis liquids being used to wash the ducts, drained and dragging condensable tar vapors with them, passing then by the condensers (Gl) where they are cooled before returning to the condensate collection tank (L1); decantation of the aqueous fraction of the pyrolytic liquids in the low temperature decanter (L3) thermally insulated with refrigeration circuits where an average duration of 8 hours is held at a temperature of 5.5 ^(, C ± 2.5 ° C, occurring the precipitation of light tars, which after passing through a charcoal filter, allows to obtain at the exit, after the time of permanence of the aqueous spinning of the pyroligneous liquids, tar contents of less than 0.2%.

2 - Installation (A) for the production of charcoal and pyroligneous liquids from woody or herbaceous plant material that includes at least one biomass cutting / fragmentation device (1) (B), at least one drying oven (2), powered by at least one mixer of hot combustion gases (2 A) and air (2B), at least four pyrolysis reactors (3), each pyrolysis reactor (3) equipped in the interior outlet with a cylindrical and removable container (3.1), ducts (3C and 3G) for vapors and pyrolysis gases, a condenser (Gl), a fan (15) that circulated the non-condensable gases that move into the gas scrubber (G2), a reservoir for collecting pyrolytic condensation liquids (L1), connected to a recirculation circuit (LA), which passes through a recirculation pump (12), a decanter (L2), a reservoir of tar (20), a reservoir of pyrolenous acid (19) and a light oil reservoir (18), characterized by comprising duct washing dispersers (13) and a low temperature dehumidifier (L3).

3 - Installation (A) according to claim 2, characterized in that the dehumidifier (L2) and the ducts (3C and 3G) constitute a recirculation circuit with dispersers (13) that inject pyrolysis liquid into the critical points of the system to prevent clogging of tar in the aforementioned pipelines (3G and 3G).

4 - Installation (A) according to claim 2, characterized in that the drying sludge (2) dries the biomass (B) by insufflating a mixture of hot combustion gases and air (2C), carried out in a turbulent manner , the hot gases coming from the furnace (3.2) of the pyrolysis reactor (3).

5 - Installation (A) according to claim 2, characterized in that the cylindrical and removable container (3.1) is removed from the furnace (3.2) with the coal inside it after pyrolysis without having to cool the pyrolysis reactor (3) and another cylindrical and removable container (3.1) filled with biomass (B) be introduced.

Installation (A) according to claim 2, characterized in that it comprises at least one pre-cooling zone (S1), a hopper (S2) for unloading coal from the removable and cylindrical container (3.1) and a tunnel with a cooling and drying system (S3) for the coal as well as a mechanical screen (S4) for separating the coal in the desired dimensions (SA1 and SA2).