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WO2018115593A1 - Conversion thermothermale de biomasse - Google Patents

Conversion thermothermale de biomasse Download PDF

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Publication number
WO2018115593A1
WO2018115593A1 PCT/FI2017/050928 FI2017050928W WO2018115593A1 WO 2018115593 A1 WO2018115593 A1 WO 2018115593A1 FI 2017050928 W FI2017050928 W FI 2017050928W WO 2018115593 A1 WO2018115593 A1 WO 2018115593A1
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WO
WIPO (PCT)
Prior art keywords
biomass
feedstock
lignin
partial wet
wet oxidation
Prior art date
Application number
PCT/FI2017/050928
Other languages
English (en)
Inventor
Karhan ÖZDENKCI
Jukka Koskinen
Cataldo DE BLASIO
Hassan Raja MUDDASSAR
Kristian Melin
Golam Sarwar
Pekka Oinas
Mika Järvinen
Original Assignee
Aalto University Foundation Sr
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Aalto University Foundation Sr filed Critical Aalto University Foundation Sr
Publication of WO2018115593A1 publication Critical patent/WO2018115593A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/40—Thermal non-catalytic treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/008—Processes carried out under supercritical conditions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0979—Water as supercritical steam
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the present invention relates to conversion of biomass to provide valuable products.
  • the present invention concerns a method of hydrothermally converting biomass, in particular lignocellulosic biomass.
  • Biomass conversion by hydrothermal processes is known in the art.
  • Hydrothermal processes use water as reaction medium, and the biomass is subjected, in the presence of water, to high temperatures and pressures to yield valuable products.
  • PWO partial wet oxidation
  • SCWG supercritical water gasification
  • HTL Hydrothermal liquefaction
  • the present invention is based on the concept of feeding biomass into a first hydrothermal unit operating at conditions of partial wet oxidation.
  • the product obtained from the partial wet oxidation is then treated in a second hydrothermal unit operating at conditions of supercritical water gasification or hydrothermal liquefaction.
  • the method can be carried out
  • the present process is mainly characterized by what is stated in the characterizing part of claim 1.
  • biomass such as lignocellulosic biomass
  • agriculture such as manure, or waste from municipalities or industry, for example sewage, such as municipal wastewater or industrial wastewater.
  • the proposed process provides a broad range of products. In fact, there is a wider spectrum than in conventional biomass processing plants.
  • profitability of the process can be further enhanced by flexible production planning based on the market need and prices.
  • the input and output can be selected to provide processing of various raw-materials to yield a great number of products.
  • the process can be integrated into a pulp mill.
  • the pulp mill can thereby be converted to the multi-product biorefinery plant.
  • the product spectrum of the mill would include lignin as a biomaterial, and bio-oil or syngas as bio-fuel or energy raw materials. Naturally, the mill will still produce pulps and paper.
  • Hydrogen-rich gas can be used as energy source to replace outsourced methane in the caustisizing section or sold as hydrogen gas.
  • Carbon dioxide -rich gas can be used in acidification for lignin recovery or transferred to algae production area.
  • thermochemical conversion reactor for example during SCWG.
  • temperatures of that reaction step can be lowered and unwanted reactions mitigated.
  • the invention also provides for energy savings.
  • PWO is an exothermic phenomenon. This reduces the amount of additional energy needed for reaching the temperature of the SCWG or HTL process in the thermochemical conversion reactor, compared to SCWG or HTL applied alone.
  • bio-oil can be upgraded to liquid biofuel or can be intermediate as the energy carrier;
  • reaction medium which gives a safe solvent for biomass processing.
  • sulphur bound to lignin is a particularly problematic form of sulphur which may not be possible to remove completely in the sulphate form as salts. Alternatively, it stays as salts in the liquid/aqueous phase.
  • one advantage of removing lignin is also to get lower sulphur content in the inlet stream to the thermochemical conversion reactor and hence in the product of this reactor as well.
  • Sectorial integration provides a more enhanced supply chain network than distributed- centralized approaches: utilizing both solid and wet biomass from various sectors (e.g. black liquor, sawdust, straw and other residues from agriculture and forestry), producing multiple products and flexible operation to adapt changes in market demand.
  • sectors e.g. black liquor, sawdust, straw and other residues from agriculture and forestry
  • Figure 1 shows a process diagram of a hydrothermal conversion process according to one embodiment
  • Figure 2 shows sectorial integration for supply chain network.
  • PWO partial wet oxidation
  • SCWG supercritical water gasification
  • HTL hydrothermal liquefaction or “subcritical liquefaction”.
  • PWO is an intermediate step serving for some energy, dissolution of suspended solid organics (if there is any) and starting to breakdown the biomass structure. Then, less energy will be needed for heating prior to SCWG or HTL and heating the reactor to maintain the temperature. In addition, any inorganic salt content can be recovered in the vertical reactor. There is lignin recovery section and the remaining liquid can be recycled since dilution of the biomass (e.g. weak black liquor) is needed anyways for the reaction process. Furthermore, the reactor can serve for both HTL or SCWG as well by adjusting pressure and temperature. This enables switching the product between syngas and bio-oil in accordance with the market demand.
  • the present technology provides a method of hydrothermally converting a biomass feedstock.
  • the method comprises the steps of subjecting the feedstock to partial wet oxidation in a partial wet oxidation unit, recovering from the unit a downstream product, and feeding at least a part of the downstream product to a thermochemical conversion reactor.
  • the product of the partial wet oxidation is subjected to supercritical water gasification or hydrothermal liquefaction to produce conversion products of the biomass.
  • the conversion products are, in particular, selected from the group of bio-oil and syngas. It should be noted that, although only one thermochemical conversion reactor is being considered in the below examples, it is possible to operate the process with two or more reactors. The reactors can be placed in serial or parallel arrangement or combinations thereof. It is also possible to operate one reactor under conditions of SCWG and another under conditions of HTL.
  • the feedstock of the process involves lignocellulosic biomasses from various sectors.
  • the feedstock spectrum covers, for example, biomasses from the forest product industry, black liquor, sawdust and woodchips being the main feedstocks; and from agricultural sector, the residues being, e.g., rice straw, wheat straw, non-wood black liquor and leaves, suitable for the proposed process.
  • the feedstock spectrum also covers lignocellulosic biomass from various other sectors, such as manure of various livestocks, is also possible.
  • waste from municipalities or industry for example sewage, such as municipal wastewater or industrial wastewater, can also be used as a feedstock.
  • wet biomass can be used as such or, in some embodiments, wet biomass blended with solid biomass or even solid biomass dispersed in aqueous phase. By feeding aqueous biomass, costs of pretreatment can be reduced.
  • the use of different raw-material sources provides for a multi-feed process.
  • Bio-oil refers to aliphatic hydrocarbons (such as alkanes) and aromatic hydrocarbons and combinations thereof which are liquid at ambient temperature and pressure (typically 25 °C and 1 bar).
  • the hydrocarbons are typically fully or partially saturated, but they can also contain unsaturation in the form of, for example, double bonds between carbon atoms. Further, the hydrocarbons may contain functional groups, such as carboxylic groups, anhydride and ester groups.
  • the liquid hydrocarbons typically have 4 to 38 carbon atoms, for example 4 to 24 carbon atoms.
  • Syngas refers to synthetic gas produced through decomposition of organic feedstock, in gas phase at the ambient temperature and pressure: containing mainly hydrogen, methane, carbon dioxide and carbon monoxide as well as lower amounts of hydrocarbons with 2 and 3 carbons (i.e. "light hydrocarbons”). There can be some water vapor or oxygen included in the syngas.
  • the syngas contains, for example at least two of the following
  • the products of the process can also contain mixtures of bio-oils and syngas.
  • One embodiment comprises producing a bio-oil formed by aliphatic, aromatic hydrocarbons or mixtures of aliphatic and aromatic hydrocarbons, which are liquid at ambient temperature and pressure; and/or syngas composed mainly of hydrogen, methane, carbon dioxide and carbon monoxide as well as lower amounts of light hydrocarbons with 2 and 3 carbons, which are gas at ambient temperature and pressure.
  • PWO partial wet oxidation
  • SCWG supercritical water gasification
  • HTL hydrothermal liquefaction
  • the PWO unit operates under oxygen partial pressure of 0.5-1.5 MPa and at a temperature in the range of 180-240 °C.
  • lignin recovery through acidification.
  • lignin precipitates when pH reduces to 9-10.
  • washing and filtering steps are typically required to get lignin as a product.
  • the other portion and residual liquid from the lignin recovery section are transferred to the thermochemical conversion reactor.
  • the thermochemical conversion reactor produces bio-oil through sub- critical liquefaction for example at a pressure of 4 to 22 MPa and at a temperature in the range of 250 to 350 °C.
  • syngas is produced through SCWG (supercritical water conditions.
  • Supercritical water gasification can be carried out at a temperature of 375 to 740 °C, for example 600 to 700 °C, and at a pressure of 25 MPa or more, for example 25 to 30 MPa.
  • supercritical water gasification is carried out for an aqueous feed containing less than 10 % of dissolved organic matter.
  • the duration of the supercritical water gasification is for example 1 to 5 minutes.
  • the energy balance of the whole process can be optimized as can the product yields.
  • the separation of the products and aqueous effluent can be performed by two -stage syngas separation or by using a drum. Based on the product demand, this conversion process can be operated in a flexible way by adjusting the flow rates and conditions in the units.
  • syngas is cooled and separated into carbon dioxide-rich and hydrogen-rich products in two stages of high- pressure and low-pressure separators.
  • the cooled product can go to low pressure separator which would function as drum in that case.
  • the aqueous effluent can also be recycled for dilution purposes as SCWG is usually implemented with less than 10 % dissolved organic content.
  • HTL process produces bio-oil as the main product and aqueous phase, char and gas as the side streams. After HTL, upgrading process is still required for bio-oil usage as fuel. Nevertheless, HTL provides bio-oil with less oxygen content compared to fast pyrolysis, thus requiring less hydrogen when upgrading. As such HTL of wood biomass is not fully competitive with petroleum-based gasoline in terms of techno-economic analysis. However, in the present combination, HTL becomes quite an interesting alternative.
  • the dry matter (solids) content of the aqueous phase subjected to HTL can be up to 40 wt-%.
  • the dry matter content is 5 to 30 wt-%.
  • the proper dry matter content can be selected depending on the feedstock.
  • Alkali such as sodium hydroxide can be added before the PWO or HTL unit.
  • the amount can be up to 60 % of feed dry matter content, typically less (10-30 wt) % of feed dry matter content.
  • the duration of the HTL is for example 1 to 12 minutes.
  • Table 1 shows examples of the range of operation conditions and the products. Table 1. Process conditions of the hydrothermal conversion process in Figure 1
  • Stream 1 is the flow of biomass feedstock, optionally liquid biomass feedstock, into the partial wet oxidation reactor 11.
  • Stream 2 is the inlet stream of oxygen and/or cooking chemicals into unit 1 1.
  • Stream 3 is the outlet (downstream product) of the partial wet oxidation reactor 11.
  • Stream 4 is the inlet feed of the SCWG or HTL reactor 18
  • Stream 5 contains the products - i.e. syngas and/or bio-oil - and water at high temperature and pressure (in practice, at the pressure and temperature of the reactor 18). Stream 5 goes to heat exchange and separation.
  • Stream 6 is the aqueous effluent remained from the separation operation of Stream 5.
  • the stream "Effluent water” is heated and recycled to the reactor as Stream 6.
  • Stream 5 has heat exchange first with the mixture of PWO and filtration downstreams (unit 15) and then the effluent water (unit 20).
  • Stream 5 can have heat exchange first with the effluent water and then with the PWO and filtration downstreams mixture.
  • Stream 7 is the lignin stream. This stream is further washed to remove the remaining inorganic solids in the lignin precipitate. The washing step is not shown in Figure 1.
  • Table 2 shows the composition of the various streams as an example of Kraft black liquor processing in case of SCWG operation in reactor 18. The calculation is based on 1 kg dry-ash-free (daf) biomass in stream 1, assuming a 20 % split to lignin recovery. The yields, compositions and conditions can slightly vary within these ranges in case of other feedstocks.
  • Table 2 also shows the elemental sulphur amounts.
  • Stream 1 contains inorganic sulphur as sulphate and sulphide, and organic sulphur bound to lignin molecules.
  • PWO oxidizes the sulphur into sulphates at least partially or even completely. Assuming complete oxidation, the same amount of sulphur as in stream 1 exists in streams 3 and 4 but in sulphate form. Inorganic sulphur is completely oxidized but organic sulphur may remain bound to lignin molecules. In case of partial oxidation sulphur, syngas with a sulphur content of less than 5 ppm can be achieved, thus still eliminating the gas-cleaning need for further usage of the gas product.
  • Stream 5 contains no sulphur (or less than 5 ppm), i.e. the gases are sulphur-free after separation.
  • a biomass feedstock having a lignin content can be fed into the partial wet oxidization and the organics partially decomposed, e.g. lignin of low molecular weight (about 100 to 5000 g/mol). This reduces the tar and char formation in the thermochemical reactor 18 compared to SCWG or HTL applied alone without PWO.
  • the plant is built as a regional biomass conversion plant for the supply chain network shown in Figure 2.
  • the conversion process is the heart of biomass supply chain networks.
  • the sectorial integration concept in Figure 2 requires multi-feedstock-multi-product processes as regional conversion of biomass, i.e. the ability to process different feedstocks from both forestry and agriculture, and multi-functional process units for flexible production.
  • the regional conversion processes can produce energy for their dedicated regions as well: for instance, syngas can be used directly for the energy need of a region.
  • hydrothermal processes are suitable for biomass, no process option alone is proven as sufficient for industrial application in terms of techno-economic performance.
  • This invention can be a solution.
  • the proposed process can be integrated with the mill and receive feedstocks from the other biomass sectors in the region as well. This will combine the benefits reduced infrastructure cost and multi-feedstock-multi-product biorefinery.
  • the sectorial integration network provides regional development as well regarding the social aspect.
  • the biomass source sites (rural areas) can provide valuable feedstock for the regional conversion processes.
  • black liquor and wood can be used in countries with a developed paper and pulp industry based on wood raw-materials, whereas an agricultural country can use agricultural and livestock residues (such as manure and straw).
  • non-wood pulp mills in agricultural places can have solution for black liquor treatment through the proposed process since the commercial recovery boiler treatment is unfeasible for non-wood mills.
  • the impact of silica on viscosity disables to concentrate the non-wood black liquor more than 50 % solid content, which results in inefficient energy production in recovery boiler.
  • non-wood black liquor can be utilized in the proposed hyrothermal process.
  • the proposed process enables multi-feedstock-multi-product and flexible operation, producing lignin and syngas or bio-oil.
  • the process uses the benefits of hydrothermal conversion methods and potentially provides energy efficient production. This process concept can also overcome the concerns of the availability of feedstock since it utilizes biomass from various sectors. The economy potential calculation determines that the process has potential for industrial implementation.
  • Multi-feed-multi-product process utilizing black liquor, saw dust, wood chips, bark, agricultural residues and possibly various manure feedstocks to produce lignin, syngas and bio-oil
  • embodiments comprise for example the following: 1. Method of hydrothermally converting a biomass feedstock selected from liquid and solid lignocellulosic feedstocks and combinations thereof, comprising subjecting the feedstock to partial wet oxidation, lignin recovery and supercritical water gasification or hydrothermal liquefaction.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)

Abstract

L'invention concerne un procédé de conversion hydrothermale d'une charge d'alimentation de biomasse, comprenant les étapes consistant à soumettre la charge d'alimentation à une oxydation humide partielle dans une unité d'oxydation humide partielle, à récupérer, à partir de l'unité, un produit aval, et à introduire au moins une partie du produit aval dans un réacteur de conversion thermochimique, où il est soumis à une gazéification d'eau supercritique ou à une liquéfaction hydrothermale pour produire des produits de conversion de biomasse. Le présent procédé peut être utilisé pour traiter la biomasse, telle que la biomasse lignocellulosique, à partir de divers domaines de l'industrie, ainsi que la biomasse provenant de l'agriculture, en vue de produire des produits de valeur, tels qu'une bio-huile et un gaz de synthèse.
PCT/FI2017/050928 2016-12-21 2017-12-21 Conversion thermothermale de biomasse WO2018115593A1 (fr)

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FI20166000 2016-12-21
FI20166000 2016-12-21

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Cited By (9)

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EP3428130A1 (fr) * 2017-07-10 2019-01-16 VPC GmbH Procédé de gazéification et de production de l'énergie électrique à partir de biomasse humide en présence deau surcritique
WO2019093949A1 (fr) 2017-11-07 2019-05-16 Kiram Ab Conversion thermochimique de biomasse
WO2020154810A1 (fr) * 2019-01-30 2020-08-06 Greenfield Global Inc. Procédé de production de kérosène synthétique
WO2021035052A1 (fr) * 2019-08-21 2021-02-25 Baudhuin Thomas J Procédé de gazéification à eau supercritique
CN114829546A (zh) * 2019-12-20 2022-07-29 塞科利亚诺蒂克公司 水热液化和湿法氧化废水处理的具有成本效益的集成
WO2022194332A1 (fr) * 2021-03-17 2022-09-22 Circlia Nordic Aps Système de pompage pour convertisseurs de biomasse thermochimiques
US20230416986A1 (en) * 2020-11-23 2023-12-28 Commissariat à l'énergie atomique et aux énergies alternatives Method for the gasification of a black liquor
US12123137B2 (en) 2019-11-08 2024-10-22 Valmet Technologies Oy Method and a system for producing an oil rich fraction from biomass
US12318765B2 (en) 2019-06-10 2025-06-03 Thomas J. Baudhuin Apparatus for supercritical water gasification

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