AT508469B1 - METHOD FOR THE THERMAL PROCESSING OF BIOMASS AND DEVICE FOR IMPLEMENTING THE PROCESS - Google Patents

Abstract

The device has a receptacle (2) for receiving catalytically active biomass (M), a transport device connected thereto (7), a storage container (20) for heating the supplied non-degassed component (R) of a reaction mixture (N) at cracking temperature (Day) for the purpose of a cracking reaction, a downstream mixer pump (24) for continuing the cracking reaction, an intermediate container (31) with Ausgasraum (29), a the intermediate container (31) downstream distillation column (30), a flow line (26 ), which leads from the outlet of the mixer pump (24) to a degassing device (28), which is arranged in the outgassing chamber (29) of the intermediate container (31), a return line (34) from the intermediate container (31) to the storage container (20). for the purpose of recycling the non-gassed component (R) of the reaction mixture (N), a condenser (38) connected to the top of the distillation column (30), in which the a cooled steam-shaped component (D ') and at the output of the generated fuel (K) is provided, a bypass (35) with bypass pump (35c), which from the lower part of the intermediate container (31) to Ausgasraum (29) leads, and a junction (35f) in the bypass (35) which is connected to the output of the transport device (7). For admixing a bottoms product obtained from the petrochemical industry, in particular vacuum gas oil (V), a container (78) is provided, the contents of which are preheated to make it liquid and / or to keep it. With this device, a relatively large amount of fuel (K) can be generated from the biomass (M).

Description

Austrian Patent Office AT508 469B1 2012-07-15

Description: [0001] The invention relates to a method for the thermal treatment of biomass according to the preamble of patent claim 1 and to a device for carrying out the method according to the preamble of patent claim 5.

Accordingly, the method is one such, [0003] a1) in which the biomass is catalytically active and is formed by a mixture of a biological residue and a biocatalyst, wherein the biocatalyst is a biologically active substance and catalytically contains active substances, a2) in which the catalytically active biomass is subjected in a storage container a cracking temperature, in particular in the range of 250 ° to 380Ό, and thereby exposed to a cracking reaction, b) in which the so-liquefied biomass optionally then in c) in which the reaction mixture thus formed is subsequently conducted into the outgassing space of an intermediate container and outgassed, after which c1) the outgassed component is cooled and provided as fuel, c2) a first portion recycled non-gassed liquid component and in the master container and optionally in the mixer pump in turn is exposed to the cracking temperature, c3) preferably a second portion of the non-degassed liquid constituent in a bypass is in turn fed to the outgassing space of the intermediate container and outgassed there, wherein fresh biomass is added to the second portion when it is fed to the outgassing space, and d) in which the residues settling in the intermediate container are collected and removed from time to time.

And in the device is such a [0005] a) with a receptacle for receiving the biomass, b) with a connected to the output of the receptacle transport device, c) with a reservoir for heating a supplied reaction mixture on crack Temperature for the purpose of a cracking reaction, d) with an optionally downstream mixer pump to continue the heat input and the cracking reaction, e) with an intermediate container with Ausgasraum, f) with an intermediate container downstream distillation column, g) with a flow line, the h) with a return line leading from the lower part of the intermediate container to the receiving container for the purpose of returning the non-gassed component of the reaction mixture, i) with a to the head of the Connected distillation column Condenser, in which the outgassed steam-shaped component cooled and at the output of the fuel produced is provided, j) preferably with a bypass with bypass pump, which leads from the lower part of the intermediate container to the Ausgasraum the intermediate container, and k) with a for the supply of biomass provided junction in the bypass, which is connected to the output of the transport device.

Such a method and such a device are known from DE 10 2008 013 241.

[0007] "Biomass" For the purposes of this and the known invention is preferably a mixture or a mixture of a relatively dry "biological residue". and a relatively dry biocatalyst ("biocatalyst"). Both the biological residue and the biocatalyst (or together) should preferably have a residual moisture of not more than 4 -12% in both cases. Both substances can be primarily those which are obtained in agriculture in large quantities as waste products. The invention presented here thus also serves primarily to eliminate biological "waste", namely by obtaining an energy source (fuel).

As "biological residue" In the present case, wood waste (eg sawdust), leaves, rape cake, sugar beet residues, pomace from beer brewing or schnapps production, solids from olive oil production, animal meal, cellulose from the Austrian patent office AT508 469 B1 2012-07-15 production of animal feed, animals, straw of wheat, barley or other cereals, or other organic substances, such as the different cereals themselves, maize, etc.

As "biocatalyst " In the present case, all bio-substances which have absorbed a certain amount of catalytically active elements, minerals or other compounds present in the soil, may also be considered. It has been proven that z. For example, a certain amount of aluminum or silicon may be referred to "biological residues". catalytically acts. Such bio-substances with mineral components are z. As rapeseed roots, rape straw or sugarcane residues (which are squeezed sugar cane).

For example, the present process is applicable to a mixture of sugar beet residues ("biological residue") on the one hand and sugarcane residues ("biocatalyst") on the other hand, or to a mixture of rape cake ("biological residue") on the one hand and rapeseed straw ( "Biocatalyst") on the other hand.

The aim of the invention is also present, to provide a method for the treatment of biomass, which allows the substantial cleavage of the organic substances contained in the biomass and the separation of the solids contained therein by thermal means. Of course, the method should also be feasible in a cost-effective manner. Accordingly, it should be possible to build the device also cost.

It is based on the knowledge and on this finding evidence experiments that the biomass as "catalytically effective biomass " should be available. Then, when exposed to thermal effects, a catalytic process begins which, with careful guidance, leads to extensive degradation of the organic substances both in the biological residue and in the biocatalyst.

The thermal catalytic effect depends on the composition of the biocatalyst. This composition can vary widely. Nevertheless, it has been found that the biological residue and the biocatalyst can be reacted in the known and in the present process so that the organic components of both substances are catalytically cracked. Back remains a solid residue that z. B. can be stored or used as a high quality residue.

It is advantageous in both methods if the fuel is dehydrated. He can then for drive machines, the z. B. are equipped with a diesel engine can be used.

The fuel can also be used to generate electricity, z. B. with the help of a turbo generator (combination of turbine and generator).

Of particular financial advantage is when the fuel is burned in a turbine and the exhaust gases of the turbine are exploited to produce the cracking temperature. In this case, the exhaust gases of the turbine can be used for heat input into a thermal oil circuit that generates the cracking temperature. The thermal oil can be supplied to the storage tank and / or a Nachheiz device.

Normally, in both methods significantly more shares of biological residue than subjected to the processing of biocatalyst.

Both methods have the great advantage that in addition to the biocatalyst and the biological residue, both of which can be considered largely as difficult to use waste, is eliminated. The further advantage is that relatively much fuel, but relatively little gas and low boilers arises. The energy content of the fuel can be used for electricity and / or heat generation for various purposes or for the operation of engines.

In the known and in the present device may be connected to the output of the capacitor, a means for the treatment of the fuel by dewatering. 2/9 Austrian Patent Office AT508 469B1 2012-07-15 [0020] The purified product is collected in a storage tank.

It is advantageous if the storage container has a double jacket through which a hot thermal oil is conductive, the temperature of which is preferably adjustable to a temperature close to the cracking temperature. In this case, the storage container may be connected to a thermo-oil circuit having a heat exchanger. Accordingly, you can proceed if a post-heating device is arranged in the bypass.

It is important that the fuel produced by a turbine for the purpose of their drive after its combustion is zuleitbar. In this case, the exhaust gases of the turbine should be guided to exploit their energy content in the heat exchanger.

Of course, the turbine may be connected to a generator. This generator can be electrically connected to the public network.

In order to achieve a high efficiency and a high yield, can also be provided that the biocatalyst and / or the biological residue of the catalytically active biomass prior to the cracking process to the ultrasound of an ultrasonic device can be suspended.

Now, experiments with the known method have shown that the non-degassed liquid, oily component that is generated in the outgassing of the intermediate container at the outgassing is also cracked because of its return to the storage tank over time, then in part is distilled from the distillation column and thus is no longer available for the process. The liquid, oil-like component must therefore be refilled from time to time to maintain the reaction in a continuous process and to keep the level in the intermediate container.

It has now been searched for a way to make refilling particularly inexpensive to maintain the reaction.

The object of the invention is therefore to provide a method and a device of the type mentioned in such a way that in a cost effective and simple way, the loss of liquid component can be compensated.

With regard to the method, this object is achieved in that in the intermediate container as Nachfüllprodukt a resulting in the petrochemical bottom product, in particular vacuum gas oil, is fed in liquid form.

The bottom products in the petrochemical industry include vacuum gas oil, bitumen and certain lubricants.

Vacuum gas oil is a mineral, fat-like product at room temperature, which is obtained as a by-product in the refinery of crude oil. It is z. B. processed to lubricant or used for drying in the thermal waste disposal, as a fuel. It is found in refineries in large quantities, so that sales difficulties exist and the product is relatively cheap. It is considered as a sort of waste product.

The present invention is based on the finding that has been confirmed by experiments that the vacuum gas oil can be advantageously used in the present process to produce fuel. It thus finds another field of application, which contributes to the reduction of the existing large supply.

The vacuum gas oil is - as I said - at room temperature, a fat-like substance, which is already oily-liquid at temperature increase to about 70 ° C. Preferably, it is preheated in the present process prior to feeding, so that it retains its liquid form or even first wins and thus enters the intermediate container. The heat for heating can be obtained from the preparation or manufacturing process of the fuel itself.

With continuous feed, the manufacturing process can be maintained for a long time. The object stated with regard to the device of the type mentioned in the introduction is achieved according to the invention in that a receptacle for a bottom product obtained in the petrochemical industry, in particular for vacuum gas Oil is provided, from which a supply line leads to the intermediate container.

In the supply line, a pump and / or a shut-off valve may be provided. For preheating, a preheater should preferably be provided. This can surround the receptacle and so the bottom product contained therein, ie z. As the vacuum gas oil, keep liquid.

Furthermore, an embodiment is advantageous in which the producible fuel for the purpose of combustion of a turbine is zuleitbar to which an electric generator is connected for the purpose of generating electrical energy, and in which the exhaust gases of the turbine are used for heating the sump product.

An embodiment of the invention will be explained in more detail below with reference to a figure. The figure shows a device in which the fuel produced by means of a catalytic treatment device from biomass is converted into electrical energy, which is fed into a public grid, while the energy content of the exhaust gases of the turbine is used for the process. Of course, the fuel can also be used for drive purposes. As a process liquid here additional vacuum gas oil is used, so this is also disposed of next to the biomass.

According to the figure, the device shown has a receptacle 2 with a lockable inlet 4 for receiving finely divided, fairly dry and catalytically active biomass M. This biomass M is produced in agriculture as a residual product. In this example, this biomass M consists of about 90% rapeseed cake as biological residue and about 10% rapeseed straw as biocatalyst.

Of course, as biomass M, another substance or substance combination of the aforementioned organic substances can be used.

At the lower end of the container 2, a metering valve 6 is arranged in an output line 5. This valve 6 is a controllable supply device, which communicates with a transport device 7 or screw for forwarding the biomass M along the output line 5 shown. Above the biomass M is in the container 2, a nitrogen pad 8 or (under low pressure) a pad of another inert gas. This ensures that no air, d. H. no oxygen in the device can penetrate. How and where the catalytically active biomass M is input into the device will be described later.

It is advantageous if in or on the output line 5 (in the sewage sludge treatment known per se) ultrasonic device 10 is arranged. By irradiation of ultrasound US into the biomass Μ, z. B. from opposite sides, it is ensured that the running off in the following cracking process is particularly effective and effective.

Of course, the catalytically active biomass M in the illustrated device itself can be prepared by mixing biocatalyst and inorganic residue.

In the present case, a feed tank 20 with double jacket 21 serves to heat the biomass M to cracking temperature T. The heat input is marked by small arrows 22. The cracking temperature T was in the investigated substances in the range of 250 ° to 380 ° C. The double jacket 21 is traversed by a hot thermal oil P.

The feed tank 20 has - as shown - preferably the double jacket 21 and is preferably arranged in a thermal oil heat cycle, wherein as thermal oil P z. As the known Meganol 420, a mineral thermal oil class 1 without special additives for high temperatures, can be used. This will be clarified later. The prevailing in the reservoir 20 temperature T is used for thermal cracking (cracking) of the organic molecules of the biomass M. Here are in the mixture M existing Austrian Patent Office AT508 469 B1 2012-07-15

Substances, especially the mineral parts of the biocatalyst, as catalysts helpful. The feed tank 20 leaves via an outlet 23, a reaction mixture N in liquid form, in which the previously existing substances have been split into a catalytic catalytic mixture to a large extent.

It may also be advantageous if a mixer pump 24 is connected to the lower outlet of the storage tank 20. This can be constructed according to FIG. 3 of DE 10 2005 056 735. The run of the mixer pump 24 is indicated by a curved arrow. The mixer pump 24 serves in particular two purposes: First, it supports the intensive mixing process of the resulting from the biomass M reaction mixture N, and secondly, it causes a shear of the existing particles and thus an increase in the surface and the efficiency.

The mixer pump 24 may itself be designed as a heater. This additional heating is marked by small wavy arrows.

The output line of the mixer pump 24 may be referred to as a flow line 26 of the ongoing reaction cycle. It is connected to an outgassing device 28, which is located in the upper part of a Ausgasraums 29 of an intermediate container 31. The intermediate container 31 is arranged in front of a distillation column 30. The outgassing device 28 serves to separate the water vapor and the organic vapors D from the liquid residues R of the reaction mixture N. The non-degassed residues R can reach the lower part of the intermediate container 31. Over time, a portion of the residues R in the form of a residue A settles on the ground. This separated residue A can be discharged into a discharge container 32 arranged there and removed from time to time. It can be disposed of by final disposal or possibly used as fuel. Water vapor and organic vapors D enter the distillation column 30.

From the lower part of the intermediate container 31, an outlet line for a first portion R1 of the not yet distilled liquid residues R leads back to the reservoir 20. This output line of the intermediate container 31 may be referred to as the return line 34 of the ongoing reaction cycle.

It should be noted that the mixer pump 24 pumps the liquid, resulting from the biomass M reaction mixture N repeatedly in the reaction cycle 24, 26, 28, 31, 34, 20. Unless new biomass M is added, this is done until practically all organic is cracked and directed upwards and until the remainder A is deposited or deposited.

It should also be noted that when starting a reaction cycle in this circuit, a high-boiling product from the process or a thermal oil V should be entered. In other words, in order to start the reaction process, the product R is added from the intermediate container 31 in hot liquid form or the thermal oil V via the line 34 of the mixture N. As will become clear later, the warm vacuum gas oil V, which is also used for another purpose, can be used for this purpose.

For continuous operation, the transported by means of the transport device 7 biomass M in a relatively small amount by means of a so-called "bypass pass 35 " fed. This bypass 35 is of particular importance. It at least reduces or prevents foaming in the intermediate container 31.

This bypass 35 comprises a return line 35a, which extends from the lower part of the intermediate container 31, a if necessary arranged thereon rehousing device 35b with double jacket, a bypass pump 35c and an outgoing therefrom supply line 35d, in an outgassing device 35e in the upper part of the intermediate container 31 above the filling level, ie in the Ausgasraum 29 ends. In this supply line 35d, the output of the transport device 7 opens at a junction 35e. The volume entered per unit time by the transport means 7 is substantially less than the volume transported by the bypass pump 35c per unit time; it is z. B. only 5% The double jacket of the after-heater 35b is also flowed through by heated ther of P thermo PERM AT508 469B1 2012-07-15 moöl.

Via the return line 35a, a second portion R2 of the residues R is withdrawn by the pump 35c. The (still relatively cold) biomass M supplied at the junction 35e is brought to a higher temperature, possibly even up to the reaction temperature T, in the end section of the feed line 35d by the residual fraction R flowing therein. All water components are converted into water vapor. This water vapor flows in the intermediate container 31 up to the distillation column 30 and then to a condenser 38, to then discharged with the fuel K and possibly from this, z. B. by means of a centrifuge to be removed.

Within the distillation column 30, the lower boiling organic vapors D 'are separated. They are withdrawn from the top of the distillation column 30. Here, therefore, a distillate line 36 is connected to the withdrawal of the top product, which leads to the condenser 38. In this condenser 38, the outgassed vaporous and lower boiling component D 'is cooled, and at its output the fuel K produced is provided in liquefied form for further utilization. This fuel K can z. B. be largely similar to the diesel oil. The cooling water lines of the capacitor 38 are designated 40, 42.

From the output of the condenser 38, a fuel duct 46 leads to a means 48 for treating the fuel K. This means 48 may preferably be used for dewatering and water removal.

The fuel line 46 then leads to a storage tank 50. From here, the fuel K can be forwarded via a fuel outlet line 52 as needed. By means of a valve 53, fuel K z. B. are removed for motor drive purposes.

In the present case, the line 52 is also connected to a turbine generator. As is known, this consists of a turbine 54 and an electric generator 56 connected via a shaft 55. In the present case, the turbine generator 54, 55, 56 is likewise used for generating electricity and for generating the cracking temperature T via a thermo-oil circuit.

According to the figure, the resulting in the combustion in the turbine 54 hot exhaust gas G is supplied via an exhaust pipe 58 to a heat exchanger 60. After cooling by thermal interaction with a thermal oil P, the exhaust gas G is discharged via an outlet line 62. It can also be used to dry the input biomass M.

The heat exchanger 60 is part of the mentioned thermal oil circuit, which is indicated only schematically. The core is a temperature controller 64, the thermal oil P in a flow line 66 to a predetermined value, which is close to the cracking temperature T, z. B. at 350 ° C, holds. The thermal oil P is introduced from the supply line 66 in the double jacket 21 of the storage tank 20 and leads here to the desired cracking temperature T. The thus somewhat cooled thermal oil P is after passing through the double jacket 21 via a return line 68 for the purpose of passage of the heat exchanger 60th attributed to this. Alternatively, depending on the temperature setting and the actual temperature and controlled by the temperature controller 64, it can be fed back into the oil feed line 66 via a bypass line 70 past the heat exchanger 60.

From the figure it can be seen that the electric generator 56 via output lines 72 in the public network, which is symbolized by a power pole 74, can feed energy. Of course, another consumer may be connected to the output lines 72.

From a container 78 via a valve 80 and possibly via a pump (not shown), a supply line 82 for vacuum gas oil to the intermediate container 31. Here, the level is kept approximately constant, so that over a long time a continuous operation is ensured. The vacuum gas oil V is in 6/9 via a preheater 76, which can surround the container 78

Claims (10)

Austrian Patent Office AT508 469 B1 2012-07-15 liquid form (ie above 70 ° C). The cost-effective vacuum gas oil V is supplied in the process shown in a simple way, used for fuel production and thereby consumed, so that here is a cheap disposal takes place. It should be noted that, in principle, another bottom product of petrochemistry, so bitumen or another lubricant can be used. It should still be stated the following: Would you only the "biocatalyst" alone? Rape straw (without rapeseed cake) submit to the present process, then you would win a lot of gas G and low-boiling products, but little diesel-like fuel K. Similarly, if only sugarcane residue ("biocatalyst") were subjected to the process. So you would the rape straw or the sugarcane residues so in order to obtain the mixture Μ z. B. with grain waste (for example, with corn waste) or mix with cellulose. In summary, it can be said that the illustrated device for fuel and / or energy production from the organic components of the starting materials biocatalyst and biological residue, which together as "catalytically active biomass M " as well as from the mineralogical bottoms product, here especially vacuum gas oil, leads, with simultaneous mass reduction. The device generally works without the addition of external catalysts. 1. A process for the thermal treatment of biomass (M), a1) wherein the biomass (M) is catalytically active and is formed by a mixture of a biological residue and a biocatalyst, wherein the biocatalyst is a bio-substance and catalytically active substances contains, a2) wherein the catalytically active biomass (M) in a master tank (20) of a cracking temperature (T), in particular in the range of 250 ° to 380 ° C, subjected and thereby exposed to a cracking reaction, b) the thus liquefied biomass (M) optionally then in a mixer pump (24) is exposed to a further cracking reaction, c) wherein the reaction mixture (N) thus formed then in the Ausgasraum (29) of an intermediate container (31) out there and there c1) the outgassed constituent (D ') is cooled and provided as fuel (K), c2) a first portion (R1) of the non-degassed liquid constituent (R) recycled and in the master tank (20) and optionally in the mixer pump (24) again the cracking temperature (T) is exposed, c3) preferably a second portion (R2) of the non-degassed liquid component (R) in a bypass (35) again the outgassing chamber (29) of the intermediate container (31) is fed and outgassed there, wherein the second portion (R2) in the supply to the Ausgasraum (29) fresh biomass (M) is added, and d) wherein in the intermediate container (31) settling residues (A) are collected and removed from time to time, characterized in that in the intermediate container (31) as a refill product in the petrochemical resulting bottom product, in particular vacuum gas oil (V) is fed in liquid form. 2. The method according to claim 1, characterized in that the feeding of the bottom product, in particular of the vacuum gas oil (V), continuously occurs. 3. The method according to claim 1 or 2, characterized in that the bottom product is preheated prior to feeding. 4. The method according to claim 3, characterized in that is used for preheating heat energy from the treatment process. 7/9 Austrian Patent Office AT508 469B1 2012-07-15 5. Device for carrying out the method according to one of claims 1 to 4, a) with a receptacle (2) for receiving the biomass (M), b) connected to the output of the receptacle (2) transport device (7), c ) with a feed tank (20) for heating a fed reaction mixture (N) to cracking temperature (T) for the purpose of a cracking reaction, d) with an optionally downstream mixer pump (24) for continuing the heat input and the cracking reaction, e ) with an intermediate container (31) with outgassing chamber (29), f) with a distillation column (30) connected downstream of the intermediate container (31), g) with a feed line (26) leading from the outlet of the mixer pump (24) to an outgassing device (28 ), which in the Ausgasraum (29) of the intermediate container (31) is arranged, h) with a return line (34) from the lower part of the intermediate container (31) to the storage container (20) for the purpose of returning the non-ausgega i) with a condenser (38) connected to the top of the distillation column (30), in which the outgassed vaporous constituent (D ') is cooled and at the outlet of which the generated fuel (K j) with preferably a bypass (35) with bypass pump (35c), which leads from the lower part of the intermediate container (31) to the outgassing chamber (29) of the intermediate container (31), and k) with one for the supply biomass (M) provided by the confluence (31 f) in the bypass (35), which is connected to the output of the transport device (7). characterized in that a receptacle (78) for a resulting in the petrochemical bottom product, in particular for vacuum gas oil (V) is provided, from which a feed line (82) leads to the intermediate container (31). 6. Device according to claim 5, characterized in that for the continuous supply of liquid bottom product, in particular of vacuum gas oil (V), in the receptacle (31) in the supply line (82) is provided a pump. 7. Device according to claim 5 or 6, characterized in that in the supply line (82) a shut-off valve (80) is provided. 8. Device according to one of claims 5 to 7, characterized in that for preheating the bottom product, in particular of the vacuum gas oil (V), a preheater (76) is provided. 9. Device according to claim 8, characterized in that the preheater (76) surrounds the receptacle (78). 10. Device according to one of claims 5 to 8, characterized in that the generated fuel (K) for the purpose of combustion of a turbine (54) is zuleitbar, to which an electric generator (56) is connected for the purpose of generating electrical energy, and that the exhaust gases (G) of the turbine (54) are used to preheat the sump product. For this purpose 1 sheet drawings 8/9