Login| Sign Up| Help| Contact|

Patent Searching and Data


Title:
METHOD AND APPARATUS FOR PREPARING FUEL FROM BIOMASS
Document Type and Number:
WIPO Patent Application WO/2014/129910
Kind Code:
A1
Abstract:
Method and apparatus for preparation of fuel from biomass wherein the biomass is subjected to a heat treatment in a temperature range from 150 to 300 C, in a reactor (11) pressurized with steam and air, wherein the pressure at completed treatment is released. The volume increase of steam and other gases from the pressure release is temporarily accumulated in a container (14) of a flexible volume while steam and other gases are subjected to heat exchange in at least one heat exchanger (13) so that condensable gases are condensed and release their heat of condensation in the at least one heat exchanger.

Inventors:
BRUSLETTO RUNE (NO)
PLÜCKHAHN WOLFGANG (DE)
Application Number:
PCT/NO2014/050024
Publication Date:
August 28, 2014
Filing Date:
February 19, 2014
Export Citation:
Click for automatic bibliography generation   Help
Assignee:
ARBAFLAME TECHNOLOGY AS (NO)
International Classes:
C10L9/08; B01D53/44; B01D53/75; C10L5/36; C10L5/44
Domestic Patent References:
WO2006006863A12006-01-19
Foreign References:
US3863710A1975-02-04
CA1141376A1983-02-15
NO320971L2006-02-20
CA1267407B1990-04-03
CN102059076A2011-05-18
Other References:
See also references of EP 2958978A4
Attorney, Agent or Firm:
CURO AS (Heimdal, NO)
Download PDF:
Claims:
Claims

1 A process for the preparation of fuels from biomass, where the biomass is subjected to a heat treatment in a temperature range from 150 to 300 °C in a reactor (11) pressurized with steam and air, wherein the pressure at the end of the heat treatment is released, characterized in that the volume increase of the steam and other gases on pressure release temporarily is accumulated in a container (14) having flexible volume, the steam and other gases being heat exchanged in at least one heat exchanger (13) so that condensable gases condense and release their heat of condensation in the at least one heat exchanger (13).

2. A method according to claim 1, characterized in that at least one container (14) with flexible volume is used downstream of the heat exchanger (13).

3. A method according to claim 1, characterized in that the heat absorbed in the heat exchanger (13), is used at least partly for preheating the supply water.

4. A method according to claim 1, characterized in that said condensable gases are collected as condensate (25) which is separated from the gas (26). 5. A method according to claim 4, characterized in that the condensate (25) is purified before discharge.

6. A method according to claim 1, characterized in that the gas passes through at least one purification step (15) before it is discharged.

7. A method as claimed in claim 6, characterized in that said purification step (15) comprises burning the combustible components, with recovery of heat from the combustion chamber and flue .gas

8. A method according to claim 1, characterized in that the biomass comprises a cellulosic material, and that at least part of the pressure release is performed abruptly to defibrate the cellulose. 9. A method according to claim 8, characterized in that the heat treatment takes place in a range between 200 and 240 °C for a time sufficient to soften the lignin.

10. A method according to claim 1, characterized in that saturated steam is used.

11. A method according to claim 1, characterized in that superheated steam is used.

12. A method according to claim 1, characterized in that the heat-treated biomass is subsequently dried.

13. A method according to claim 1 or 12, characterized in that the heat-treated biomass is pelletized. 14. A method according to claim 1, characterized in that the heat treatment takes place in a time period of 1-30 minutes.

15. A method according to claim 1, characterized in that biomass with a moisture content between 10 and 60% is used.

16. An apparatus for the preparation of fuel from biomass, where the biomass is subjected to a heat treatment in a temperature range from 150 to 300 °C in a reactor (11) pressurized with steam and air, wherein the pressure at the end of the heat treatment is released, comprising a reactor (11) for the heat treatment and a pressure release tank (12) which receives the material after the treatment, characterized in further comprising: at least one heat exchanger (13) for gas which leaves the pressure release vessel and at least one container (14) having flexible volume for temporary accumulation of non-condensed gases discharges from the pressure release tank (12).

Description:
Method And Apparatus For Preparing Fuel From Biomass

The present invention is related to method and apparatus for improving the manufacturing costs and the reduction of emissions to the air in the preparation of fuels from biomass. Background

Pellets produced from biomass are increasing with regard to production of thermal electricity as replacement for coal and is thus a contributor to reduction of C0 2 emissions. In recent years, pellet production has been dominated by production without heat treatment of the biomass, thus producing so-called first generation pellets or "white pellets". Now focus is changing production of so-called second generation pellets where the biomass is heat treated to change the properties of the biomass. One of these methods utilizes so-called steam explosion method, where biomass is heat treated with steam.

In pellets production which uses steam explosion method as method for heat treatment, such as described in Patent 320 971, or by other related methods of heat treating biomasses or so called ligno-cellulosic material, these methods involve emissions to air which have not been considered adequately. The steam explosion method for pressurizing a container of the supplied biomass and then pressurizing with steam supply, with following instantaneous discharge, also provides a discharge of steam and volatile gases from the mass having being heated.

There are also existing and expired patents that deal with steam treatment of biomass or so-called lignocellulosic materials. These mainly conclude that it is advantageous to apply steam (saturated or superheated steam) to a closed container I which biomass have already been supplied and heating it to a given temperature in the temperature range from 160 degrees up to 300 degrees, depending on the what you want to achieve in the reactor, and then emptying the reactor in one or two steps. It is part of the prior art to vary the degree of filling of the reactor, to vary moisture of supplied biomass, and to calculate the associated, required amount of steam to both heat the biomass (dry material + moisture in the mass) and to create the desired pressure / temperature relationship in the reactor. Typical operation ranges are between 150 and 280 degrees Celsius, but it turns out that the preferred properties for energy purposes are best achieved if the temperature is held between 190 and 235 degrees Celsius, or approximately a pressure from 15 to 28 bars. When heating the moist biomass in a pressure vessel in which steam is supplied, the steam will condense on the particles to transfer energy to the biomass, and its moisture is heated to the desired temperature range. In addition an amount of steam has to be supplied to achieve the desired total pressure and temperature of the atmosphere surrounding the biomass. A challenge with this system is that it uses quite a lot of energy to produce the required amount of steam (in the order of 200-600 kg steam per ton of material). A certain amount of biomass is supplied to which the amount of steam to be added is determined as a function of the filling level of the reactor, of the desired pressure and temperature, of the inlet temperature and of the moisture level of the mass to be treated. When there is little mass volume in a reactor, less steam is required to be heated than when more mass is present in the same container/ reactor, and drier mass requires less steam to be heated than a wetter material, while the desired pressure/ processing temperature will subsequently affect the total steam demand.

Emptying the reactor can be done by emptying in one or more steps, as described in Norwegian patent No. 320,971, Canadian Patent No. 1,267,407 (De Long) or others. One can thus reduce the so-called expulsion pressure to a lower level than the desired operation pressure. This expulsion pressure can be from 1-3 bars up to the processing pressure depending on what is actually desired to achieve. If it is just for emptying the reactor, a lower expulsion pressure is desirable, and if a defibration or a "bursting" of the fibers is desired, a higher expulsion pressure is desired, i.e. greater pressure difference between the reactor and the site to which the mass is discharged (often close to atmospheric pressure or slightly higher in order to reduce the volume).

Emptying / discharge of biomass from a reactor can proceed in the form of a flow through a pipe or passage, expanding towards a volume of lower pressure, where the mass is separated from the steam, so that the mass remains in the tank/ separator/ cyclone while the steam expands out in the open. Emptying occurs rapidly, the driving force being the pressure difference. The greater the pressure difference the greater the amount of steam emitted simultaneously with the mass to be used further. When this occurs a large amount of energy is thus released. This energy should preferably be recovered.

During the heat treatment volatile gases (volatiles) are released from the biomass and are mixed with steam and contaminate the steam. The gases produced are mainly organic acids and aldehydes, which are discharged and produced with time. The amount of gas depends on time, temperature and pressure. The primary and predominant initial reaction is the decomposition of hemicellulose to, for example, furfural, formic acid, acetic acid. A plethora of gas components have been observed in the mixture. These gases have different boiling points and are either soluble in water or insoluble in water at different temperature ranges. Several of these gases have a strong odor that is characteristic of the method and many find the smell unpleasant, and it also contains a lot of carbon remains that should rather be reused. The general problem with heat recovery associated with this type of process is that a large amount of gas and steam are discharged within a few seconds, why there are high demands on heat exchange unit, and in addition the product flow is very complex where volatile (non -condensable) and condensable gases come with a little predictable mass composition. This can lead to a build up of pressure downstream of the process that interferes with the mass flow. In addition to this comes the fact that many of the components are crude in the sense that they have a strong odor and can lead to physical discomfort for personnel who are exposed to them.

Object

It is an object of the present invention to provide a method and an apparatus for producing fuel from biomass in such a way that energy is being recycled to a larger extent and the disadvantage in the form of unpleasant odors is reduced or eliminated.

The present invention

The above objects are achieved by the present invention which according to a first aspect is comprised by a method as defined by claim 1.

According to a further aspect the present invention comprises an apparatus as claimed in claim 16. Preferred embodiments of the invention are disclosed by the dependent claims.

The invention is a method and an apparatus that provides advantages inter alia in pellets production which makes use of the steam explosion method, by allowing energy recovery of the discharge steam while at the same time allowing elimination of the odor problem that is inherent with gases (VOCs) that accompany the steam in the discharge composition. The container with flexible volume can be a container with flexible walls, or a container having at least one movable wall, such as a cylindrical container with a wall in the form of a movable piston.

Final treatment of the biomass in the form of drying and optional pelletization is not further described here as this can be done in various ways known in the art and does not constitute part of the present invention. Detailed description of the invention

In the following, the invention is further described by way of non-limiting examples of embodiments with reference to the accompanying drawings.

Figure 1 shows an apparatus in accordance with the present invention in a certain stage of the process.

Figure 2 shows the apparatus of Figure 1 in another step of the process.

Figure 1 illustrates from left to right, a reactor 11 for heat treatment of wood/ pulp/ cellulose- containing material. In the reactor 11 is the mass is heated under pressure in the presence of water vapor and air. The mixing ratio between water vapor and air may vary and the filling level of the reactor can likewise vary.

Temperature and residence time in the reactor may vary and are typically in the range from 160 to 300 ° C and from 1 to 15 minutes. Higher temperatures and longer processing time are as controlling elements actually undesirable because it provides greater degradation, more mass loss and problems in operating the downstream process in the form of undesirable amounts of non- condensable gases, gases with strong odors, etc.

The reactor will typically comprise equipment and devices for controlling and monitoring the process, including valves to control pressure, means for heating and cooling of the reactor respectively, etc. This is not illustrated since it is not a main issue of the present invention how the process is run in reactor 11. Container 12 is a pressure release vessel into which the reaction mixture is released at end of treatment. At least a portion of the pressure in the reactor 11 is released abruptly, thereby expelling the reaction mixture from the reactor into the pressure release container 12.

The skilled artisan will appreciate that gases other than steam and air may be present in the reactor, provided that they do not interfere negatively with the process quantities. For example, the ratio between oxygen and nitrogen in the reactor be different from what is the case in air, e.g. through the addition of oxygen enriched air or oxygen consumed during the process.

On completion of reaction treatment the reaction mixture is expelled from the reactor 11 to pressure release tank 12 via conduit 21. This is performed in a manner known in the art and as such does not represent anything new. The solid with a certain quantity of moisture is moved into the pressure release tank 12 and transferred via conduit 22 to after-treatment in any suitable manner known in the art. The gas containing condensable components as well as components which are not condensable within the prevailing conditions, passes through conduit 23 at or near the top of the pressure release tank 12 and is led therefrom directly to at least a heat exchanger 13.

The heat exchanger 13 cools the gas flow and ensures that the condensable components of the gas are condensed, so as to thereby reduce the volume of the gas flow. The heat of condensation received by the refrigerant is utilized as energy in any suitable manner within or outside the current process. Typically, this energy is used to preheat the air for a drying unit or for

combustion. The condensate from the heat exchanger 13 contains, in addition to water, components which should be removed before the water is discharged or recycled for reuse. The condensate is discharged through conduit 25, while the gas passes to the next step in the process through conduit 26.

As regards the heat exchanger or heat exchangers 13 this or these can be indirect heat exchangers where the refrigerant is kept separate from the vent gases or it can be direct heat exchangers where cooling water is mixed with the vent gases. It can also be a combination, where the heat exchange mainly is indirect, but where water 24 at a limited rate is sprayed into the flow of discharge gases into the heat exchanger 13 to cause a quenching of the discharge gases 23 to thereby more easily condense all condensable components in the subsequent indirect step of heat exchange.

If one chooses to use only direct heat exchange, a much larger volume of fluid needs to be handled downstream of the heat exchanger. It is therefore preferred that the heat exchange at least partially is conducted as indirect heat exchange.

The next step of the process consists of a container 14 with flexible volume, typically a "balloon", which like other balloons has soft walls and is dimensioned so that it is able to receive the "puff" of non-condensable gases resulting from expulsion from a batch reactor operated under normal operating conditions. In Figure 1, the reaction mixture is still enclosed in the reactor 11 and container 14 with flexible volume is therefore substantially empty, as is shown in the figure.

Referring now to Figure 2, which shows the same as Figure 1 except that here the pressure in the reactor has just been released so that the reaction mixture has been expelled into the pressure release tank 12 while the gas is blown on to the container 14 with flexible volume through the heat exchanger 13 and conduits 23 and 26. Within a few seconds after the pressure is released, the container 14 is inflated by non-condensable gases as shown in Figure 2. The container 14 will typically be oversized in relation to the need that can be calculated based on a single batch. In addition, a safety valve can ensure that the container 14 does not burst even in case of extreme amounts of non condensable gases. The container 14 will, for each batch, for a short period of time, occupy the entire amount of non-condensable gases without thereby causing any significant overpressure, and then slowly and in a controlled manner release the gas via conduit 27 to at least one chamber 15 for after-treatment of the gases, ensuring that the gases do not escape to the atmosphere untreated. Here any flammable components may be burned and the combustion heat may be taken care of through appropriate cooling of the chamber and/ or of the exhaust gases.

After-treatment can be conducted in multiple chambers 15, arranged in series, parallel or a combination of series and parallel. This is not essential to the present invention. What is important is what takes place in the form of heat exchange in heat exchanger(s) 13 and temporary accumulation of non-condensable gases in a container 14 with flexible volume. This combination is unique and indicates that the heat energy that one previously was not able to take care of in this type of batch processes, now is possible to recover in order to achieve a process with a lower net energy consumption and thereby a more profitable process. In addition one achieves the bonus that gases with harmful or unpleasant odors are taken care of. It is furthermore possible to reduce the load on the heat exchanger by placing a container with flexible volume upstream thereof, to reduce the rate at which released gases pass through the heat exchanger. The disadvantage of this is that all "unclean" components will still be present in the gas and parts of these will adhere to the walls of the container 14 with the flexible volume.

With regard to the need for dimensioning, a typical reactor for the purpose in question can have a volume of 10 m 3 and with a pressure of 25 bars, the pressure release will produce up to approx. 250 m 3 gas that needs to be taken care of. In practice, the amount of gas will be somewhat less because part of the reactor volume is occupied by the biomass and because some of the pressure can be vented out carefully prior to the sudden pressure release. By appropriately controlling of the process, the volume which is discharged in one quick pressure surge lasting approximately for 5 seconds, may be decreased to approximately 70 m 3 . The specific heat of vaporization of water is 242 kJ/ mole or 13.45 MJ/ kg. If 50% of these 70 m 3 is water vapor (about 1 kg/ m 3 ), the immediate need for heat transfer in heat exchangers will amount to:

35kg/5sek x 13.45 MJ/ kg = 95 MW provided all available vapors will condense. The processes can naturally be controlled so that this need larger or smaller, the figures given as an example of sizing needs, but also to shed light on the challenges of success in managing such energy-rich "impacts". If condensation capacity is not sufficient a pressure build-up will take place. The prerequisite for respite and escape out through the condensing unit is that the capacity is so large that the pressure drop does not increase excessively.

The part of the reduction of the steam impact caused by introduction/ self-production of volatile gases, means that the impact of non-condensable gases is increased to a volume of from 25 to 150 m 3 per ton biomass or up to 30 m 3 per second. This must be considered a large useless volume in relation to the reactor size. This pressure impact is large and must be collected and then passed on as a continuous flow. To collect a large quantity of gas in a short time at such a low pressure, is a demanding task which according to the present invention is solved by the container with the flexible volume. After-treatment must also be performed on both water and gas. This is made according to known technology once the process is carried out in accordance with the present invention.

Example

If the desired reactor is 10 m 3 and this is supplied with 5 m 3 of biomass (wood chip or similar) then that corresponds to a ton of mass

Variation of moisture in reactor per ton mass

Dry matter 400 600 700 900 Kg

Spec heat wood mass 0,65 0,65 0,65 0,65 Kcal/kg

Degrees

Diff temp 145 145 145 145 Celsius

enthalpy 37700 56550 65975 84825 Kcal

Water 600 400 300 100 Kg

Spec heat water 1 1 1 1 Kcal/kg

diff temp 145 145 145 145 degrees

enthalpy 87000 58000 43500 14500 Kcal

sum Kcal 124700 114550 109475 99325 sum kcal

Required energy 514,8 472,9 451,9 410,0 GJ / ton Required amount of steam

In addition, steam is needed to provide a desired vapor pressure

Filling level 50% means that approximately 70% of the volume is filled with steam to provide steam pressure, and at a reduction/ expulsion pressure of 10 bars, there will be 75 kg steam in the reactor.

Required amount of steam to obtain the vapor pressure; 75% of the volume * 10 bar * lkg/m 3 = 75 kg

From this we can calculate volume of the puff and volume of non-condensable gases.

Per ton mass supplied

Moisture as water 600 100 kg

enthalpy 350 350

Enthalpy water 306346 111741

Dry matter 400 900

Spec enthalpy TS 228 228

Enthalpy TS 91000 204750

Sum Diff enthalpy 397346 316491

kg evaporated 212 169

As moisture

increase 63 50

pressure 75 75

Sum Puff 287 244 kg

Mass loss becomes

NCG 100 100 kg

This means that for a typical volume and operation rangel80-235 ° C, the condensable volume is 25-35 times the reactor volume and the non-condensable gases corresponds to the mass loss in the reactor, ranging from 0-30 times the reactor volume. Both volumes are slightly changed when it turns out that the mass loss becomes both water and non-condensable gases depending on the pressure/ time / temperature in the reactor. The example shows that the immediate impact is huge.