EP3523404A1 - Procédé de carbonisation hydrothermale de boues dans des usines de pâte chimique - Google Patents

Procédé de carbonisation hydrothermale de boues dans des usines de pâte chimique

Info

Publication number
EP3523404A1
EP3523404A1 EP17858813.3A EP17858813A EP3523404A1 EP 3523404 A1 EP3523404 A1 EP 3523404A1 EP 17858813 A EP17858813 A EP 17858813A EP 3523404 A1 EP3523404 A1 EP 3523404A1
Authority
EP
European Patent Office
Prior art keywords
sludge
htc
pulp mill
fraction
reactor
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP17858813.3A
Other languages
German (de)
English (en)
Other versions
EP3523404A4 (fr
Inventor
Fredrik Lundqvist
Erik ODÉN
Fredrik ÖHMAN
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
C Green Technology AB
Original Assignee
C Green Technology AB
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 C Green Technology AB filed Critical C Green Technology AB
Publication of EP3523404A1 publication Critical patent/EP3523404A1/fr
Publication of EP3523404A4 publication Critical patent/EP3523404A4/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/403—Solid fuels essentially based on materials of non-mineral origin on paper and paper waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/086—Hydrothermal carbonization
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/26—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof
    • C02F2103/28—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof from the paper or cellulose industry
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present disclosure relates generally to the treatment of sludge generated in chemical pulp mills, and in particular to a method and system involving a step of hydrothermal carbonization of said sludge, feeding the resulting solids and liquid fractions to the power boiler and recovery boiler respectively, and thus integrating the sludge handling in the steam generation for the pulp mill.
  • Sludge a slurry of solids and water, including dissolved material, is what remains after wastewater treatment in municipal and industrial wastewater treatment plants.
  • Industrial wastewater treatment plants treat water effluents from different industrial processes, for example pulp and paper mills, industrial food production facilities etc. All wastewater treatment plants in use generate sludge that needs to be handled in one way or the other.
  • the sludge is either recovered directly from the plant after dewatering (aerobic sludge) or first treated
  • biosludge anaerobically for biogas production where part of the sludge is digested and the remainder is recovered as anaerobic sludge, also called biosludge.
  • the wastewater treatment generates large volumes of sludge.
  • biosludge is a considerable problem and carries significant specific costs per ton sludge treated.
  • the sludge can be incinerated in the power boiler of the pulp mill, contributing to the production of steam necessary for the pulp and paper making process. This has the advantage of avoiding that the inorganic content of the sludge is introduced into the closed pulp mill cycle. With suitable treatment of flue gases and ashes, harmful chemicals and heavy metals can be neutralized or even recovered. Sludge with high concentrations of organic and/or biological
  • Another alternative is combustion in the recovery boiler. Sludge is first hydrolysed with heat and alkali and then mixed with black liquor before feeding the mixture to the evaporators to increase its dry solids content before combustion in the recovery boiler.
  • An advantage of this alternative is that a multi-effect evaporation plant can be used to dewater the sludge before combustion in the recovery boiler, and the energy content of the sludge is utilized. This however often requires a pre-hydrolysis treatment where alkali is charged.
  • the ash from the sludge contains inert components such as phosphorus and silica which will accumulate in the lime cycle and give rise to an increased make-up lime demand. Additionally, the amount of spent lime that has to be handled will increase.
  • NPEs non-process elements
  • aluminum, calcium, iron, potassium and chlorides which can cause problems in the pulp mill, such as corrosion, fouling, worse dewatering properties of green liquor dregs and lime mud etc.
  • the sludge can be designated for external use, for example as landfill or landfill cover, as fertilizer or as soil replacement products.
  • This represents a costly and environmentally less attractive treatment, as it includes the transport of large volumes of material with high moisture content.
  • Methane is a greenhouse gas, and although it doesn't linger as long in the atmosphere as carbon dioxide, it is initially far more
  • Hydrothermal carbonization also known as wet torrefaction is a thermochemical process used in the production of charred matter similar in composition to coal. It involves subjecting a wet, carbohydrate feedstock, such as sludge, to an elevated temperature (180 °C - 350 °C) and pressure (up to 2.- 5 MPa) in a closed system.
  • a wet, carbohydrate feedstock such as sludge
  • pressure up to 2.- 5 MPa
  • bio char a product which is friable, hydrophobic, and has a significantly increased energy density compared to the starting material.
  • WO 2015/025076 (Valmet Technologies Oy) relates to the application of a HTC process in a pulp mill. According to the application, lignin is separated from a lignin containing liquid medium, such as pulp mill black liquor, and subjected to further treatment.
  • the method comprises at least the following steps: a) a precipitation stage, wherein a pH lowering agent is added to the lignin containing slurry for precipitating lignin, b) followed by a first separation stage, wherein the precipitated lignin is separated as a lignin cake from the remaining liquid phase of the lignin containing slurry, c) a suspending stage, wherein the lignin cake is suspended for obtaining a lignin suspension, d) a hydrothermal carbonization stage, wherein the lignin suspension is treated for obtaining a slurry of carbon containing material, and e) a second separation stage, wherein the carbon containing material is separated from the slurry.
  • a first aspect relates to a method for treatment of sludge in a chemical pulp mill including a step of hydrothermal carbonization (HTC) of a sludge stream, wherein
  • HTC hydrothermal carbonization
  • a HTC arrangement comprising a HTC reactor and subjected to elevated temperature and pressure, producing at least one solids fraction, at least one liquid fraction, and at least one gaseous fraction;
  • said at least one solids fraction is fed to a power boiler of said pulp mill and burned to generate steam;
  • said at least one liquid fraction is combined with weak black liquor from the pulp mill and fed to a black liquor evaporator of said pulp mill, and
  • said at least one gaseous fraction from said HTC arrangement is combined with air and the resulting mixed gas fed into the power boiler.
  • the liquid fraction is subjected to oxidation before it is combined with black liquor.
  • part of the steam generated by the power boiler is used to heat one or more of the HTC arrangement, the HTC reactor or the inflow of sludge to said reactor and/or arrangement.
  • the elevated temperature in said HTC step is a temperature in the interval of 180 - 350 °C, preferably 180 - 300 °C, and most preferably 180 to 230°C.
  • the pH in the hydrothermal carbonization reaction is controlled, most preferably to a pH above 5.
  • the chemical pulp mill operates according to the kraft process (the sulfate process).
  • the sludge in question is the biosludge from the treatment of wastewater from said pulp mill.
  • the sludge can also be a combination of sludge from the pulp mill and sludge from other sources, for example from municipal waste water treatment.
  • a second aspect relates to a system for treatment of sludge from a chemical pulp mill, comprising a hydrothermal carbonization (HTC) arrangement, comprising a HTC reactor, wherein said system further comprises
  • At least one separation arrangement in or downstream of said HTC reactor for producing at least one solids fraction, at least one liquid fraction, and at least one gaseous fraction
  • a feeding arrangement for feeding said at least one solids fraction to a power boiler of said pulp mill
  • the system comprises an arrangement for combining said at least one gaseous fraction with air and feeding the resulting mixed gas into said power boiler.
  • the system comprises a heater arranged to receive steam from said power boiler.
  • said heater is adapted to heat said HTC reactor or to heat the inflow of sludge to said reactor.
  • the chemical pulp mill operates according to the kraft process (the sulfate process).
  • the sludge in question is biosludge from the treatment of wastewater from said pulp mill.
  • the sludge can also be a combination of sludge from the pulp mill and sludge from other sources, for example from municipal waste water treatment.
  • the system is housed in a mobile unit, preferably a shipping container.
  • Fig. 1 schematically illustrates how the HTC process can be integrated in a chemical pulp mill
  • Fig. 2 schematically shows components of the HTC arrangement, the HTC reactor and auxiliary equipment.
  • Sludge and in particular biosludge contains comparatively high concentrations of inorganic compounds that are unwanted in the process (non- process elements, NPEs). Even though the biosludge is a small stream compared to e.g. the wood intake to the pulp mill, the high concentration of NPEs leads to a significant total intake to the pulp mill.
  • Johan Dahlbom discusses the effects of NPEs in the chemical recovery system of a kraft pulp mill [Dahlbom, J., protagonist av PFG vid indunstning och forbranning av bioslam i ett massabruks sodapanna (English translation: Effects of Non Process Elements in the chemical recovery system of a kraft pulp mill from the incineration in the recovery boiler of biological sludge), Rapport 798, Varmeforsk Service AB, S2- 226, 2003].
  • Dahlbom investigated the relative contribution of NPEs in biosludge to the overall intake in a Swedish pulp mill. His results are shown in Table 1.
  • HTC hydrothermal carbonization
  • a first aspect relates to a method for treatment of sludge in a chemical pulp mill including a step of hydrothermal carbonization (HTC) of a sludge stream, wherein
  • HTC hydrothermal carbonization
  • a HTC arrangement comprising a HTC
  • said at least one solids fraction is fed to a power boiler of said pulp mill and burned to generate steam;
  • said at least one liquid fraction is combined with weak black liquor from the pulp mill and fed to a black liquor evaporator of said pulp mill, and
  • FIG. 1 A general embodiment of the integration of a HTC process in a chemical pulp mill is illustrated in Fig. 1 where a sludge stream (A) is fed to a HTC arrangement (HTC) from which the resulting liquid fraction (B) is fed to the black liquid evaporators of the pulp mill, and mixed with thin black liquor, sometimes also referred to as weak black liquor.
  • the resulting solids fraction is then combusted in the recovery boiler.
  • the resulting steam can be used to heat the evaporators and also for other energy needs in the pulp mill.
  • the resulting solids fraction (C) is fed to the power boiler of the pulp mill, preferably together with the HTC off-gas (D).
  • a fraction (E) of the steam generated by the power boiler can be used for heating the HTC arrangement, the HTC reactor or the incoming sludge.
  • the HTC arrangement preferably comprises several components as schematically illustrated in Fig. 2.
  • the dashed line delimits the HTC
  • a HTC reactor (10) is shown as the central component of the HTC arrangement.
  • Sludge (A) is fed into the HTC arrangement in to equipment (50) for receiving and diluting the sludge, for example a tank with a mixer.
  • the sludge can then be pre-heated in a pre-heater (60) which can be any type of suitable heat exchanger, such as a double-tube or a tube-and-shell type heat exchanger.
  • the pre-heater (60) is preferably heated by steam (E) from one or more flash recovery steps (30).
  • a final heater (70) is preferably provided immediately before the HTC reactor (10).
  • the final heater (70) is preferably heated by steam (F) from the power boiler.
  • the choice of type, configuration and dimension of the pre-heater and final heater can be made by a skilled person.
  • a solids fraction and a liquid fraction are withdrawn directly from the HTC reactor (not shown).
  • a single liquid HTC product is withdrawn from the HTC reactor (10) and subjected to separation in one or more steps.
  • it is first subjected to a step of flash evaporation (30), also referred to as flash steam recovery, followed by another step of solids / liquid separation (40).
  • the flash evaporation step produces steam (E) which can be used to pre-heat the incoming sludge.
  • the second step of solids / liquid separation (40) can be chosen from a sedimentation step, a filtering step, a filter press, a solids / liquid separator screw or compactor, or the like.
  • the solids fraction is concentrated to an interval of 60 - 75 % DS and the liquid fraction will contain less than 10 % DS.
  • Said HTC reactor (10) also produces off-gas which preferably is fed to a condenser (20) supplied with a cooling liquid (G) which can be water.
  • the condensate is recirculated to the sludge receiving and dilution step (50) and the off-gas (D) is preferably fed to the power boiler and combusted.
  • the off- gas can be mixed with air, preferably compressed air, before feeding to the power boiler.
  • the HTC arrangement shown within the dashed line in Fig. 2 is only an example of how the HTC step can be integrated in a pulp mill.
  • the sludge stream referred to is a sludge stream generated in the chemical pulp mill, or a combination of different sludge streams, at least some of which are generated in the chemical pulp mill.
  • the sludge can thus be a combination of sludge from the pulp mill and sludge from other sources, for example from municipal waste water treatment.
  • sludge from the chemical pulp mill is used to produce an energy-rich solid product with high dry solids content which can be fired efficiently in the bower boiler of the mill and used to generate steam and power for the mill.
  • most of the inert components, such as P and Si are contained in the solid product.
  • the pH in the hydrothermal carbonization reaction is controlled, most preferably to a pH above 5, by the addition of suitable alkaline compounds (e.g. black liquor, spent lime mud).
  • suitable alkaline compounds e.g. black liquor, spent lime mud.
  • elements such as Ca and P will start to dissolve to a greater degree in the process water.
  • Further pH adjustments for example increasing the pH to neutral or alkaline pH, are preferably performed to influence the distribution of NPEs between the HTC liquid and HTC solids fraction.
  • the liquid from the hydrothermal carbonization which normally contains about 15-30% of the organic material, is sent to the pulp mill evaporation plant, where it will be evaporated and combusted together with the black liquor.
  • An advantage is that its energy content will generate at least enough steam to drive the evaporation and very likely also generate a surplus for the pulp process.
  • the liquor In the hydrothermal carbonization process, the liquor will be heated up to around 90 °C, thus requiring very little preheating when it is introduced into the evaporator train.
  • the liquid from the hydrothermal carbonization is subjected to oxidation before being combined with the black liquor.
  • the oxidation step is performed at a temperature in the interval of 180 - 300 °C, preferably 230 to 300°C, by the injection of an oxidizing agent into said first fraction.
  • Said oxidizing agent is preferably chosen from oxygen, hydrogen peroxide, percarbonate, and percarbonic acids, and preferably an oxygen containing gas, such as air, most preferably compressed air.
  • said at least one gaseous fraction from the HTC reactor is combined with air and fed to the power boiler. This has the advantages that it adds fuel to the boiler; it ensures destruction of possible organic residues in the HTC gas; and minimizes costs for gas treatment in the HTC plant.
  • part of the steam generated by the power boiler is used to heat the HTC reactor or the inflow of sludge to said reactor.
  • the elevated temperature in said HTC step is a temperature in the interval of 180 - 350 °C, preferably 180 - 300 °C, most preferably 180 - 230°C.
  • the chemical pulp mill operates according to the kraft process (the sulfate process).
  • said sludge is biosludge from the treatment of wastewater from said pulp mill.
  • the sludge can also be a combination of sludge from the pulp mill and sludge from other sources, for example from municipal waste water treatment.
  • a second aspect relates to a system for treatment of sludge from a chemical pulp mill, comprising a hydrothermal carbonization (HTC) reactor, wherein said system further comprises
  • the system comprises an arrangement for combining said at least one gaseous fraction with air and feeding the resulting mixed gas to said power boiler.
  • the system comprises a reactor for oxidation of the liquid fraction, as well as auxiliary equipment for feeding an oxidizing agent into said reactor, and equipment for recovering heat generated in said oxidation.
  • auxiliary equipment for feeding an oxidizing agent into said reactor, and equipment for recovering heat generated in said oxidation.
  • Such equipment can comprise a compressor for injecting compressed air into the liquid fraction.
  • a vapor-liquid separator or flashing arrangement for cooling the oxidized liquid can also be included.
  • the chemical pulp mill operates according to the kraft process (the sulfate process).
  • said sludge is biosludge from the treatment of wastewater from said pulp mill.
  • the sludge can also be a combination of sludge from the pulp mill and sludge from other sources, for example from municipal waste water treatment.
  • the system is preferably integrated in the pulp plant, for example built into and fully integrated in new plants, or as an add-on to existing plants.
  • the system is housed in a mobile unit, preferably a shipping container. This is preferably placed in close proximity to the power boiler.
  • the HTC product is combusted in the mill power boiler at high dry solids content to generate steam to drive the HTC process as well as a steam surplus that can be used in the mill.
  • the HTC liquid is evaporated together with the black liquor and the dissolved organics are combusted in the recovery boiler generating enough steam to drive the evaporation.
  • the energy content of the sludge is efficiently used, while at the same time avoiding the problems related to NPE intake to the closed cycle of the chemical pulp mill.
  • Including a step of oxidation of the liquid fraction makes it possible to extract heat in the form of steam from the liquid fraction, contributing to the heating requirements of the pulp mill or to the heating requirements of the HTC process.
  • the oxidation step also makes it possible to reduce the liquid volume before mixing with the black liquor. Additionally, the oxidation step will result in chemical reactions in the liquid fraction, for example decomposing various chemical substances.
  • Example 1 HTC-treatment of biosludge from a Swedish pulp mill
  • Biosludge from a Swedish pulp mill was treated with hydrothermal carbonization at a temperature of 200 °C in a stirred 0.5 I batch reactor. Biosludge was loaded into the reactor and heated to the carbonization temperature. After carbonization, the reactor was rapidly cooled, and the resulting slurry filtered. Separate analyses were made of the solid and liquid product to determine the distribution of NPEs in the respective phase.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Mechanical Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Treatment Of Sludge (AREA)
  • Paper (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

L'invention concerne un procédé et un système pour le traitement de boues dans une usine de pâte chimique, comprenant une étape de carbonisation hydrothermale (HTC) d'un flux de boues, ledit flux de boues étant introduit dans un agencement de HTC et soumis à une température et à une pression élevées, ce qui produit au moins une fraction solide, au moins une fraction liquide et au moins une fraction gazeuse ; ladite fraction de solides étant introduite dans une chaudière de production d'énergie de ladite usine de pâte et brûlée pour générer de la vapeur ; ladite fraction liquide est combinée à de la liqueur noire faible provenant de l'usine de pâte et introduite dans un évaporateur de liqueur noire de ladite usine de pâte et la liqueur noire concentrée résultante est brûlée dans une chaudière de récupération de ladite usine de pâte.
EP17858813.3A 2016-10-05 2017-09-26 Procédé de carbonisation hydrothermale de boues dans des usines de pâte chimique Withdrawn EP3523404A4 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE1651305A SE540135C2 (en) 2016-10-05 2016-10-05 Method for hydrothermal carbonization of sludge in chemical pulp mills
PCT/SE2017/050932 WO2018067055A1 (fr) 2016-10-05 2017-09-26 Procédé de carbonisation hydrothermale de boues dans des usines de pâte chimique

Publications (2)

Publication Number Publication Date
EP3523404A1 true EP3523404A1 (fr) 2019-08-14
EP3523404A4 EP3523404A4 (fr) 2020-06-17

Family

ID=61827305

Family Applications (1)

Application Number Title Priority Date Filing Date
EP17858813.3A Withdrawn EP3523404A4 (fr) 2016-10-05 2017-09-26 Procédé de carbonisation hydrothermale de boues dans des usines de pâte chimique

Country Status (6)

Country Link
EP (1) EP3523404A4 (fr)
JP (1) JP2019537674A (fr)
BR (1) BR112019006748A2 (fr)
CL (1) CL2019000893A1 (fr)
SE (1) SE540135C2 (fr)
WO (1) WO2018067055A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113307467A (zh) * 2021-05-12 2021-08-27 贵阳学院 一种污泥生物炭土壤改良剂生产装置

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108911478A (zh) * 2018-07-12 2018-11-30 四川深蓝环保科技有限公司 一种两阶段污泥水热反应装置
CN109279751A (zh) * 2018-11-13 2019-01-29 天津城建大学 一种剩余污泥的预处理方法和应用
SE542967C2 (en) * 2018-11-26 2020-09-22 C Green Tech Ab Method for hydrothermal carbonization and wet oxidation of sludge
CN217677380U (zh) * 2020-08-17 2022-10-28 深圳清研紫光检测技术有限公司 生物质水热碳化全量资源化处理与再利用系统和耦合系统
CN114956991B (zh) * 2021-11-08 2023-12-05 昆明理工大学 一种造纸污泥水热冶金并联产有机酸的方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011004398A1 (de) * 2011-02-18 2012-08-23 Siemens Aktiengesellschaft Verfahren und Reaktor zur hydrothermalen Karbonisierung von Biomasse
DE102013217418A1 (de) * 2013-05-08 2014-11-13 Siemens Aktiengesellschaft Hydrothermale Behandlung von Abwasserschlamm und Schwarzlauge
FI20135842L (fi) * 2013-08-19 2015-02-20 Valmet Technologies Oy Menetelmä ja järjestelmä ligniinin käsittelemiseksi
DE102014103704A1 (de) * 2014-03-18 2015-09-24 Ava-Co2 Schweiz Ag Vorrichtung zur ortsunabhängigen Behandlung von Biomasse

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113307467A (zh) * 2021-05-12 2021-08-27 贵阳学院 一种污泥生物炭土壤改良剂生产装置

Also Published As

Publication number Publication date
EP3523404A4 (fr) 2020-06-17
CL2019000893A1 (es) 2019-08-02
WO2018067055A1 (fr) 2018-04-12
SE1651305A1 (en) 2018-04-06
SE540135C2 (en) 2018-04-10
JP2019537674A (ja) 2019-12-26
BR112019006748A2 (pt) 2019-06-25

Similar Documents

Publication Publication Date Title
WO2018067055A1 (fr) Procédé de carbonisation hydrothermale de boues dans des usines de pâte chimique
JP4888911B2 (ja) 有機性廃棄物の処理設備および処理方法
CN1099386C (zh) 处理污水的方法
CN102950137B (zh) 一种餐厨垃圾的协同处理方法
US10836666B2 (en) Method for oxidation of a liquid phase in a hydrothermal carbonization process
CN202865076U (zh) 一种生物质污泥处理系统
CN104176883B (zh) 造纸废水资源化处理系统及相应工艺
KR101853734B1 (ko) 유기성폐기물 음폐수의 처리수 무방류 자원화 처리장치 및 그 처리방법
KR20200077310A (ko) 하수 슬러지를 이용한 메탄가스 제조장치 및 방법
JP2008212860A (ja) 廃棄物処理設備
CN118139825A (zh) 一种使用消化液处理水和有机干物质的混合液生产沼气的系统
CN100503015C (zh) 利用锅炉烟道尾气治理造纸黑液的工艺
US11999921B2 (en) Hydrothermal carbonization of sludge including recycling of a wet-oxidized fraction
WO2017222462A1 (fr) Procédé d'oxydation d'une phase liquide dans un procédé de carbonisation hydrothermale
Leghari et al. Research advancements in nutrients and heavy metals, its speciation and behavior during hydrothermal carbonization of sludge–A critical review
Hu et al. Wet air oxidation (WAO) on sludge treatment and its first industrial application in China
Rulkens et al. Recovery of energy from sludge–comparison of the various options
KR20160033967A (ko) 유기성 폐기물 감량처리 및 에너지생산 시스템
EP2746231A1 (fr) Procédé et appareil pour le traitement de l'eau de traitement provenant d'un processus de conversion de matériau organique hydrothermique
CN210193783U (zh) 一种造纸废水厂化学污泥制备脱硫剂的装置
KR102619461B1 (ko) 유기성 폐기물을 활용한 바이오가스 생산시스템
EP1112971A1 (fr) Procede de production d'un carburant organique liquide et sans soufre
JP2024152114A (ja) 処理システム
JP2024006246A (ja) 水熱炭化処理を用いた有機性廃棄物の処理方法、および水熱炭化処理を用いた有機性廃棄物の処理設備
CN115010316A (zh) 一种造纸废料的处理工艺

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20190404

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAV Request for validation of the european patent (deleted)
DAX Request for extension of the european patent (deleted)
A4 Supplementary search report drawn up and despatched

Effective date: 20200518

RIC1 Information provided on ipc code assigned before grant

Ipc: C02F 11/18 20060101ALI20200512BHEP

Ipc: C02F 11/10 20060101ALI20200512BHEP

Ipc: C10L 5/40 20060101ALI20200512BHEP

Ipc: D21C 11/00 20060101ALI20200512BHEP

Ipc: C10L 9/08 20060101AFI20200512BHEP

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20210401