PRODUCTION OF PRODUCTS FROM BIOMASS

Abstract

A process for producing products from biomass comprises pyrolysing biomass at a selected temperature and producing a bio-syngas, processing bio-syngas from pyrolysis step (a) to remove condensable constituents from the bio-syngas, and processing the non-condensable bio-syngas from bio-syngas processing step (b) and producing one or more than one product, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics.

Claims

1. A process for producing products, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics, from biomass that comprises the following steps: (a) pyrolysing a feed material in the form of biomass at a selected temperature and decomposing the feed material and producing a bio-syngas and a solid char, (b) processing bio-syngas from pyrolysis step (a) to remove condensable constituents from the bio-syngas and producing a condensed bio-liquid, such as a bio-tar, and a non-condensable bio-syngas; and (c) processing the non-condensable bio-syngas from bio-syngas processing step (b) in a bio-hydrocarbons synthesis process step and producing one or more than one product, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics.

2. The process defined in claim 1 wherein the selected temperature for the pyrolysis step (a) is >500° C.

3. The process defined in claim 1 wherein the selected temperature for the pyrolysis step (a) is >600° C.

4. The process defined in claim 1 wherein the bio-liquids includes bio-tar.

5. The process defined in claim 1 includes a drying step of drying the feed material for the pyrolysis step (a) to a required moisture content for the pyrolysis step.

6. The process defined in claim 1 includes a cooling step for bio-syngas when an end use of bio-syngas is for use as an engine fuel and/or for direct combustion.

7. The process defined in claim 6 wherein the cooling step includes a gas storage (buffer) step.

8. The process defined in claim 1 includes transferring O.sub.2 from the bio-hydrocarbons synthesis process step (c) to the pyrolysis step (a) to substitute at least a part of the air that would otherwise be needed to cobust an energy source to generate heat for the pyrolysis step (thus, eliminating or minimising N.sub.2).

9. The process defined in claim 1 includes enriching the bio-syngas by “cracking” bio-liquids produced in the process, thereby enriching bio-syngas with more CH.sub.4, C.sub.2H.sub.4, and C.sub.2H.sub.6.

10. The process defined in claim 1 includes mixing (i) char from the pyrolysis step (a), (ii) bio-liquids from the bio-syngas processing step (b) and (iii) optionally water and forming a paste product.

11. A plant for producing products, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics, from biomass that includes: (a) a pyrolyser unit for pyrolysing a feed material in the form of biomass at a selected temperature and decomposing the feed material and producing a bio-syngas, (a) a bio-syngas condenser for condensing bio-liquids (such as bio-tars) from the bio-syngas from the pyrolysis unit and producing (i) condensed bio-liquids and (ii) a non-condensable bio-syngas; and (b) a bio-hydrocarbon synthesis unit for producing one or more than one product, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics, from the bio-syngas.

12. The plant defined in claim 11 wherein the pyrolyser unit is also adapted to produce char.

13. The plant defined in claim 11 wherein the pyrolyser unit includes a combustion unit for generating heat for pyrolysing the feed material.

14. The plant defined in claim 13 wherein the combustion unit is adapted to operate with air, O.sub.2 or O.sub.2-enriched air.

15. The plant defined in claim 11 wherein the bio-hydrocarbon synthesis unit is configured to produce O.sub.2.

16. The plant defined in claim 15 being configured to transfer O.sub.2 produced in the bio-hydrocarbon synthesis unit to the combustion unit.

17. The plant defined in claim 11 wherein the selected temperature for the pyrolyser unit is a high temperature of >500° C.

18. (canceled)

19. The plant defined in claim 11 includes a paste product unit for producing the paste product from char from the pyrolyser unit, bio-liquids from the bio-syngas condenser unit, and optionally water.

20. (canceled)

21. A process for producing products from biomass comprises pyrolysing biomass at a selected temperature and producing a bio-syngas, processing bio-syngas from pyrolysis step (a) to remove condensable constituents from the bio-syngas, and processing the non-condensable bio-syngas from bio-syngas processing step (b) and producing one or more than one product, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics.

22. A process for producing products from biomass that comprises pyrolysing biomass at a selected temperature and producing a bio-syngas, with the pyrolysis step including selecting pyrolysis operating conditions, such as temperature and residence time, to optimize the required gas composition for a direct end-use application for the bio-syngas.

Description

DESCRIPTION OF FIGURES

[0122] The invention is described further by way of example only with reference to the accompanying Figures, of which:

[0123] FIG. 1 is a flow sheet that summarises an embodiment of the process and production plant of the present invention;

[0124] FIG. 2 is a bar chart of mass yield of pyrolysis products residual solid char, bio-syngas (referred to as “volatile” in the Figure) and bio-liquid (referred to as “bio-oil” in the Figure) during pyrolysis test work on biomass carried out at 400° C., 500° C., and 600° C.;

[0125] FIG. 3 is a bar chart of the compositions of bio-syngas produced during pyrolysis test work on biomass carried out at 400° C., 500° C., and 600° C.;

[0126] FIG. 4 is a bar chart of heating value (lower heating value (“LHV”) and higher heating value (“HHV”)) of bio-syngas produced during pyrolysis test work on biomass carried out at 400° C., 500° C., and 600° C.;

[0127] FIG. 5 is a flow sheet that summarises another, although not the only other, embodiment of the process and production plant of the present invention; and

[0128] FIG. 6 is a drawing that illustrates an embodiment of an overall sustainable commercial system that includes the process and plant of the flow sheet of FIG. 1 and biomass production that feeds biomass into the flow sheet and downstream processing options.

DESCRIPTION OF EMBODIMENTS

[0129] The following description of embodiments of the invention is divided into the following sections: [0130] FIG. 1 embodiment (including a series of sub-headings). [0131] Summary of experimental work. [0132] FIG. 5 embodiment. [0133] FIG. 6 embodiment.

FIG. 1 Embodiment

[0134] An embodiment of the process and the production plant 3 of the present invention is described with reference to the flowsheet of FIG. 1.

[0135] The process shown in the flowsheet of FIG. 1 produces products, such as bio-fuels, bio-chemicals, bio-solvents and bio-plastics from a source of bioenergy that includes biomass from wood waste or other sources of biomass. The process comprises the following steps: [0136] (a) drying a feed material in the form of a wood waste biomass and/or other biomass in a drying unit 7 to a suitable moisture content for a pyrolysis step in the process and producing (i) dried feed material (compared to the input feed material—typically 10-15% moisture) and (ii) water; [0137] (b) pyrolysing the dried feed material at a selected temperature, such as but not necessarily at a low temperature of <500° C., typically 300-500° C., and typically at higher temperatures of >500° C., more typically >550° C., typically under fast pyrolysis (flash pyrolysis) conditions in a closed system pyrolyser unit 5 that avoids forming or minimises forming light fractions and decomposing the feed material and producing (i) a solid char output and (ii) a bio-syngas output, [0138] (c) processing bio-syngas from pyrolysis step (a) in a bio-syngas condenser unit 9 and producing (i) non-condensable bio-syngas (typically CO, H.sub.2, N.sub.2, and CH.sub.4 and other hydrocarbons, such as C.sub.2H.sub.4 and C.sub.2H.sub.6) and (ii) condensed constituents of the bio-syngas as bio-liquids (referred to as bio-tar in the Figure); [0139] (d) processing non-condensable bio-syngas from the bio-syngas condenser unit 9 and producing products, such as bioenergy (referred to as bio-fuels in the Figure), bio-chemicals, bio-solvents and bio-plastics from bio-syngas processing step (b), for example by processing the bio-syngas in a bio-hydrocarbons synthesis unit 17, such as a Fischer Tropsch or other process unit, for example catalyst-based units; and [0140] (e) processing bio-tar from the condenser 9 and producing products that can be used as sources of energy.

[0141] The key focus of the process of the embodiment is to maximise the production of bio-syngas (typically CO, CO.sub.2, H.sub.2, N.sub.2, and CH.sub.4 and other hydrocarbons, such as C.sub.2H.sub.4 and C.sub.2H.sub.6) from biomass in the pyrolysis step and to process bio-syngas by removing condensable constituents and producing bio-syngas that is processed further as required to suit selected end-use applications to form products, such as bio-chemicals, bio-fuels, bio-solvents, and bio-plastics. Having said this, the embodiment also makes use beneficially of the char produced in the pyrolyser unit 5 and the bio-liquids produced in the bio-syngas condenser unit 9.

[0142] Specifically, typically the operating conditions for the pyrolysis step (a) are selected so that at least 80 wt. %, typically at least 85 wt. %, typically at least 90 wt. %, of the output of the pyrolysis step (a) is bio-syngas.

[0143] The selection of the temperature for the pyrolysis step (a) is one relevant operating condition. Typically, higher temperatures of >500° C., more typically >550° C., and more typically again >600° C. are required to increase the bio-syngas output for the pyrolysis step (a).

[0144] Other relevant operating conditions include, by way of non-limiting example, the properties of the feed material and residence time in pyrolysis step (a).

[0145] The process makes it possible to produce bio-chemicals, bioenergy (such as bio-fuels), bio-solvents, and bio-plastics with very low concentrations of inorganics.

[0146] In the case of bio-fuels, this means that the bio-fuels are suitable for use as a fuel source for engines.

[0147] More particularly, the process includes the following steps: [0148] (a) grinding a part of the char output from the pyrolyser unit 5 in a suitable mill (not shown); [0149] (b) processing bio-syngas from the pyrolysis step by condensing condensable constituents in the bio-syngas condenser unit 9 and producing a bio-liquid and a non-condensable bio-syngas; and [0150] (c) mixing the ground char from the pyrolysis step, the bio-liquid from the bio-syngas processing step, and optionally water in a mixing unit and forming a paste product in a paste product mixing unit 21.

[0151] The moisture released in the drying unit 7 is transferred to a condenser unit 13 and the liquid water from the condenser unit 13 is transferred to and used as at least part of the water input to the paste product mixing unit 21.

[0152] A part of the char output from the pyrolyser unit 5 is combusted in a combustion unit 11 and the output heated combustion gases are used to provide heat for the pyrolyser unit 5 via indirect heat exchange.

[0153] The flowsheet also shows examples of possible downstream uses of the paste product from the paste product mixing unit 21 and the bio-syngas produced in the bio-syngas condenser unit 9. These downstream uses include: [0154] (a) using the paste product as a source of energy in a combustion unit 19 or a modified internal combustion engine; and [0155] (b) using the bio-syngas from the bio-syngas condenser unit 9 in bio-chemicals production, specifically a bio-hydrocarbons synthesis unit 17, such as a Fischer Tropsch or other process unit, and producing (i) bio-chemicals, bio-fuels, bio-solvents, and bio-plastics and (ii) O.sub.2, with the O.sub.2 being beneficially used in the plant.

[0156] Features of the embodiment shown in the flowsheet of FIG. 1 are as follows: [0157] Water evaporated from the dryer unit 7 is used in the process for higher efficiency and/or in downstream processes. [0158] Gas from the combustion unit 11 or a modified internal combustion engine 19 can be used within the process—specifically, in the dryer unit 7 for higher efficiency. [0159] Cooled heating gas (from the pyrolyser unit 5) can be used within the process—specifically, in the dryer for higher efficiency. [0160] The pyrolyser unit 5 is indirectly heated. [0161] The O.sub.2 by-product from the Fischer Tropsch or other suitable process unit 17 can be used as an oxidant for the combustion unit for the indirectly heated pyrolyser unit 5. As noted above, this use of oxygen as a substitute for air is beneficial for the process. [0162] The dryer/pyrolysis unit combination 5, 7 can easily be controlled to vary moisture content during pyrolysis. This provides unique control of composition of exit gases. (i.e. “bio-syngas”—the CO and H.sub.2 ratios, etc.). [0163] Products of the pyrolysis unit include: [0164] Solid (char). [0165] Liquid (pyrolysis hydrocarbons). [0166] Gas (bio-syngas). [0167] Initial calculations are that the usable, high grade energy produced is about 1.5 MWt per tonne of wood waste biomass. [0168] The char may have some “activated carbon” properties, excellent for use in catalysis.

Biomass

[0169] The elemental composition of wood waste biomass and other types of biomass differs based on where these species are grown.

[0170] Compared to other solid fuels such as coal, wood waste biomass has higher volatile and oxygen content, but low heating value and fixed carbon content.

[0171] Additionally, the sulphur content in wood waste biomass is small, mostly less than 0.5 wt. %. In addition, typically the inorganics in wood waste biomass are also generally very low.

[0172] The main components of wood waste biomass are cellulose, hemicellulose, and lignin, each of which is different in their decomposition behavior.

[0173] The decomposition of each element occurs in a different temperature range and depends on heating rate, particle size and presence of the contaminants. Hemicellulose is the easiest one to be pyrolyzed, next would be cellulose, while lignin is the most difficult one.

Products of Biomass Pyrolysis

[0174] The two primary products obtained from pyrolysis of wood waste biomass and other types of biomass in the embodiment of FIG. 1 are solid char and bio-syngas. The bio-syngas is condensed to remove condensable constituents as a dark brown viscous bio-tar, leaving a non-condensable bio-syngas. The condensed bio-tar is a useful source of energy.

Char

[0175] Thermal degradation of lignin and hemicellulose in wood waste biomass in the embodiment of FIG. 1 results in a considerable mass loss in the form of volatiles, leaving behind an amorphous carbon matrix which is referred to as bio-char.

[0176] Depending on the biomass and the pyrolysis conditions in the pyrolysis unit 5, 10 to 35% biochar is produced.

[0177] It has been reported in the technical literature that three different temperature regions produce different char yields during pyrolysis, as follows: [0178] 450-500° C. (Low-temperature zone): char quantity was high due to low devolatilization rates and low carbon conversion. [0179] 550-650° C. (Moderate-temperature zone): char reduced dramatically. The maximum yield in this region was found to be about 8 to 10% of biochar [0180] >650° C. (High-temperature zone): char yield was very low.

[0181] The properties of char depend on pyrolysis as well as feedstock conditions.

[0182] Generally, the following characteristics can be observed during biochar production: [0183] 1. Char physical characteristics are much affected by pyrolysis conditions such as reactor type and shape, biomass type and drying treatment, feedstock particle size, chemical activation, heating rate, residence time, pressure, the flow rate of inert gas, etc. [0184] Pyrolysis operating conditions such as higher heating rate (up to 105-500° C./s), shorter residence time and finer feedstock produce finer char whereas slow pyrolysis with larger feedstock particle size results in a coarser char. [0185] Crop residues and manures generate a finer and more brittle structured char in pyrolysis processes. [0186] 2. Char mainly consists of carbon along with hydrogen and various inorganic species in two structures: stacked crystalline graphene sheets and randomly ordered amorphous aromatic structures. The C, H, N, O and S are commonly combined as heteroatoms that influence the physical and chemical properties of biochar. However, composition, distribution and proportion of these molecules in biochar depend on a variety of factors including source materials and the pyrolysis methodology used.

Bio-Syngas

[0187] Temperature and moisture content affect the bio-syngas production in the pyrolysis unit 5 through heat transfer processes.

[0188] Bio-syngas produced in the pyrolysis unit 5 comprises H.sub.2, CO, CH.sub.4, CO.sub.2, water vapour (H.sub.2O), nitrogen (N.sub.2) and light hydrocarbons such as C.sub.2H.sub.4 and C.sub.2H.sub.6.

[0189] The amount and the composition of the bio-syngas (and the amount of char) produced in the pyrolysis step 5 is a function of pyrolysis conditions, such as temperature and residence time.

Bio-Liquids, Such as Bio-Tar

[0190] Bio-liquids, such as bio-tar produced from the condensation of bio-syngas from the pyrolyser unit 5, have the following advantages:

[0191] Bio-liquids, such as bio-tar, are transportable.

[0192] A high energy density—a useful source of energy.

Biomass Pyrolysis Units 5

[0193] The pyrolysis unit 5 options include, by way of example only: Bubbling fluidized bed.

[0194] Fixed bed reactor.

[0195] Circulating fluidized bed.

[0196] Ablative reactor.

[0197] Rotating cone reactor.

[0198] PyRos reactor.

[0199] Auger reactor.

[0200] The above embodiment is an effective and efficient embodiment of maximizing energy recovery from biomass.

Summary of Experimental Work

[0201] Extensive test work in relation to the invention has been carried out in the Chemical Engineering Department of Monash University, Melbourne, Victoria, for the applicant.

[0202] The test work included but was not limited to the experimental work summarized below: [0203] Flash and slow pyrolysis of biomass under an inert environment was conducted in a bespoke pyrolysis unit operating either as a fixed bed reactor or as a fluidised bed reactor depending on the particle size of biomass supplied to the pyrolysis unit. [0204] The size of the biomass particles was in a range of 200 μm to 2 mm. [0205] Pyrolysis temperatures were in a range of 400° C.-600° C. and pyrolysis was carried out at atmospheric pressure. [0206] The gas residence time inside the main vessel varied from 2-10 seconds depending on the operation mode and operating conditions (i.e. temperature and residence time). [0207] The feed biomass was dried to 10-15% moisture before being supplied to the pyrolysis unit. [0208] The feed rate of biomass to the pyrolysis unit was 30-50 g/min. [0209] Three types of pyrolysis products, namely bio-syngas, solid char, and bio-liquid were collected and analysed for composition and other characteristics. [0210] Pollutants emission analysis was also performed.

Pyrolysis Unit

[0211] The pyrolysis unit comprises (a) an electrically heated furnace, (b) a main vessel positioned within the furnace a feed assembly and having a reactor chamber for up to 5 kg of dry biomass (during batch operation), and (c) a separate condenser unit (including a chiller) for condensing and collecting liquid from bio-syngas discharged from the reactor chamber. [0212] The pyrolysis unit includes a temperature controller for controlling the temperature in the reactor chamber. [0213] The pyrolysis unit has a programmable control system. The unit can be operated either in batch mode or continuous operation mode. [0214] As noted above, the pyrolysis unit can be operated as a fixed bed or a fluidised bed. [0215] The electrically heated furnace is capable of heating the reactor chamber to temperatures in a range of 200-800° C. [0216] The biomass residence time inside the main vessel was varied from 2-10 seconds depending on the operation mode and operating conditions. [0217] The feed system is designed with screw feeder system. The feeding rate was varied between 1 kg˜3 kg/hr (i.e. 17 g/min-50 g/min). [0218] The chiller is capable of reducing the condenser temperature from 0-20° C. depending on the operation mode and operating conditions [0219] The pyrolysis unit is integrated with a micro-gas chromatograph that monitored the bio-syngas composition in real time.

Biomass

[0220] The biomass was E. Eucalyptus nitens. The biomass was wet (around 70-80% moisture). The biomass was air dried and ground to a particle size range of 200 μm to 2 mm, Normally, grinding biomass to a size less than 2 mm is too energy intensive.

Flash Pyrolysis Mode of Operation

[0221] In flash pyrolysis mode of operation, biomass was fed directly to the pre-heated reactor chamber.

[0222] During the experiments, the reactor chamber was pre-heated to 400° C. 500° C. or 600° C. Biomass was fed inside the reactor at 1 to 3 kg/hr (17-50 g/min). If the temperature remained constant, the gas composition, solid char, and liquid yields did not vary with feed rate. All the experiments were conducted at atmospheric pressure under inert atmosphere, with nitrogen being used as the inert gas. After each experiment, the amount of solid char inside the reactor chamber was measured. The bio-syngas released for the reactor chamber was calculated form the feed rate and other measurements.

Slow Pyrolysis Mode of Operation

[0223] In slow pyrolysis mode of operation, the reactor chamber was operated in a batch mode program. 3 kg d biomass (10% moisture) was supplied to the reactor chamber. The temperature of the reactor chamber heated to 400° C., 500° C. and 600° C. at a constant heating rate of 5° K/min. Nitrogen was used as inert gas for mass balance purposes. A trace gas is needed to do a proper mass balance, Nitrogen was used as the trace gas because it does not contribute to any reactions during pyrolysis. The nitrogen flow rate and the bio-oil collection rate are known. Integrating the measured flow data (mole fraction of gases from a micro GC) over the experimental time gives the total yield of bio-oil and bio-syngas. The sum of total yield of bio-oil, bio-syngas and solid char inside the reactor chamber makes total 3 kg of dry biomass). The nitrogen flow is calculated so that both in batch and continuous process, the gas residence time remains the same inside the reactor chamber.

Operating Procedure

[0224] The standard operating procedure was almost same for batch and continuous experiments. [0225] Wet biomass is dried until (10-15% moisture) and ground to a desired particle size and loaded to the feeder unit (for continuous operation) or directly into the reactor chamber (for batch operation). [0226] The reactor chamber was pre heated to the desired temperature (for continuous operation) or heated at a controlled rate from room temperature to the desired temperature (for batch operation). [0227] Purge nitrogen gas was used only for batch process. [0228] 17˜50 g/min of biomass was fed (for continuous operation). [0229] The condenser was chilled to 10° C. for bio-oil condensation and collection form the bio-syngas from the pyrolysis unit. [0230] Char residue was collected from the reactor chamber after each experiment.

Analytical Equipment

[0231] A thermogravimetric (TGA) analyser and a CHNSO analyser were used for elemental analysis. [0232] A gas chromatography-mass spectrometry (GC-MS) was for analysis of bio-oil,

Experimental Results in FIGS. 2-4

[0233] The data presented in the Figures is the average of two experiments at each temperature,

[0234] The gas data presented is the average of 5 individual gas chromatograph measurements for each experiment. The error is 2-5% during the measurements.

[0235] The results of the experimental work are summarized in FIGS. 2-4 and, as follows: [0236] It was observed that the bio-syngas composition produced in the reactors did not vary with feed rate. [0237] The compositions of the bio-syngas were a function of temperature. [0238] High temperature reduces solid yield and boosts bio-syngas yield. [0239] The heating value of the bio syngas can be increased if pyrolysis temperature is high (600° C. in this case). [0240] CO.sub.2 can be reduced if the pyrolysis temperature is above 600° C. [0241] H.sub.2, CO and CH.sub.4 contents can be increased if biomass is pyrolyzed at higher temperatures, such as 600° C.

FIG. 5 Embodiment

[0242] The embodiment of the process and production plant of the present invention shown in FIG. 5 for biomass conversion to fuel/power/chemicals is based on the data generated from the experimental work described above.

[0243] The flow sheet shown in FIG. 5 is a more specific flow sheet than the more general flow sheet shown in FIG. 1 and the same reference numerals are used in both Figures to describe the same operating units.

[0244] More particularly, the FIG. 5 flow sheet is a selection of unit operation options in the FIG. 1 flow sheet. The following description focuses on these selections.

[0245] In addition, in basic process terms, the two flow sheets have the same focus of selecting the operating conditions of the pyrolysis step to optimize/maximise non-condensable bio-syngas production compared to solid char production and to minimize bio-liquids (bio-tar in the Figure) production in the bio-syngas condenser 9 downstream of the pyrolysis unit 5. Based on the experimental work described above higher temperatures of >500° C., more typically >550° C., and more typically again >600° C. are required to increase the bio-syngas output for the pyrolysis unit 5.

[0246] With reference to FIG. 5, the bio-syngas from the bio-syngas condenser 9 is split onto two portions.

[0247] One portion is transferred to the gas engine/turbine 19 and is combusted with an air/O.sub.2 mixture to generate work/power and a hot flue gas stream. The work/power is used as required in downstream applications. The hot flue gas stream is transferred to the drying unit 7 and used to dry feed biomass to a pre-determined moisture content for the pyrolysis unit 5.

[0248] The other portion of the bio-syngas is transferred to the bio-hydrocarbons synthesis unit 17, such as a Fischer Tropsch or other process unit, and produces (i) bio-chemicals, bio-fuels, bio-solvents, and bio-plastics and (ii) O.sub.2, with the O.sub.2 being beneficially used in the gas engine/turbine 19.

[0249] It is noted that the flue gas (CO.sub.2, H.sub.2O, and N.sub.2) from the drying unit 7 is cleaned and then used beneficially in the bio-hydrocarbons synthesis unit 17. The bio-tar from the bio-syngas condenser 9 is used as an energy source in the combustor 11 for the pyrolysis unit 5.

[0250] The above embodiment is an effective and efficient embodiment of maximizing energy recovery from biomass.

FIG. 6 Embodiment

[0251] FIG. 6 is a drawing that illustrates an embodiment of an overall sustainable commercial system that includes the process and plant of the flow sheets of FIG. 1 and FIG. 2 and biomass production that feeds biomass into the flow sheet and downstream processing options.

[0252] With reference to FIG. 6, the system includes the following elements: [0253] (a) a source of biomass, such as forests, etc. that produces biomass—with the biomass production being renewable and sustainable and acting as a CO.sub.2 sink; [0254] (b) using the biomass as a feed input to the process and plant of the flow sheets of FIG. 1 and FIG. 2 and for other uses including building materials and food; and [0255] (c) using the bioenergy product, bio-hydrocarbon product, and the oxygen by-product from the process and plant of the flow sheets of FIG. 1 and FIG. 2 beneficially within the process/plant and for other end uses.

[0256] Many modifications may be made to the embodiment of the invention described above without departing form the spirit and scope of the invention.

[0257] By way of example, whilst the embodiment includes processing bio-syngas in a Fischer Tropsch process unit, the invention is not confined to this process unit and extends to the use of any suitable bio-hydrocarbons synthesis unit for processing the bio-syngas to produce end-sue products.

[0258] By way of further example, whilst the embodiments include a bio-syngas condenser unit 9, the invention is not so limited and extends to situations in which the bio-syngas produced in the pyrolysis unit 5 is used directly, i.e. without separating bio-syngas from the pyrolysis unit 5 into condensable and non-condensable constituent streams in the bio-syngas condenser unit 9, in downstream applications, for example as an energy source for a burner, such as a steam boiler. In this context, it is preferred that the operating conditions, such as temperature and residence time, for the pyrolysis unit 5 be selected to optimize the required gas composition for the direct end-use application.