JP2015522106A5 - - Google Patents
Download PDFInfo
- Publication number
- JP2015522106A5 JP2015522106A5 JP2015521981A JP2015521981A JP2015522106A5 JP 2015522106 A5 JP2015522106 A5 JP 2015522106A5 JP 2015521981 A JP2015521981 A JP 2015521981A JP 2015521981 A JP2015521981 A JP 2015521981A JP 2015522106 A5 JP2015522106 A5 JP 2015522106A5
- Authority
- JP
- Japan
- Prior art keywords
- particles
- chamber
- gasification chamber
- gas
- char
- 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.)
- Granted
Links
- 238000002309 gasification Methods 0.000 claims description 59
- 239000002245 particle Substances 0.000 claims description 54
- 238000000034 method Methods 0.000 claims description 41
- 239000003575 carbonaceous material Substances 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 238000000197 pyrolysis Methods 0.000 claims description 12
- 235000013339 cereals Nutrition 0.000 claims description 4
- 238000005336 cracking Methods 0.000 claims description 4
- 239000010871 livestock manure Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 239000010902 straw Substances 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 241000219310 Beta vulgaris subsp. vulgaris Species 0.000 claims description 2
- 241001474374 Blennius Species 0.000 claims description 2
- 229920000742 Cotton Polymers 0.000 claims description 2
- 241000195493 Cryptophyta Species 0.000 claims description 2
- 240000003133 Elaeis guineensis Species 0.000 claims description 2
- 235000001950 Elaeis guineensis Nutrition 0.000 claims description 2
- 210000003608 Feces Anatomy 0.000 claims description 2
- 235000019735 Meat-and-bone meal Nutrition 0.000 claims description 2
- 240000007594 Oryza sativa Species 0.000 claims description 2
- 235000007164 Oryza sativa Nutrition 0.000 claims description 2
- 241000209504 Poaceae Species 0.000 claims description 2
- 241000219000 Populus Species 0.000 claims description 2
- 240000000111 Saccharum officinarum Species 0.000 claims description 2
- 235000007201 Saccharum officinarum Nutrition 0.000 claims description 2
- 241000218998 Salicaceae Species 0.000 claims description 2
- 240000001016 Solanum tuberosum Species 0.000 claims description 2
- 235000002595 Solanum tuberosum Nutrition 0.000 claims description 2
- 240000006394 Sorghum bicolor Species 0.000 claims description 2
- 235000011684 Sorghum saccharatum Nutrition 0.000 claims description 2
- 244000269722 Thea sinensis Species 0.000 claims description 2
- 240000008042 Zea mays Species 0.000 claims description 2
- 235000002017 Zea mays subsp mays Nutrition 0.000 claims description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- 235000005822 corn Nutrition 0.000 claims description 2
- 235000005824 corn Nutrition 0.000 claims description 2
- 239000000835 fiber Substances 0.000 claims description 2
- 230000005484 gravity Effects 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims description 2
- 229920005610 lignin Polymers 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 235000013622 meat product Nutrition 0.000 claims description 2
- 235000014571 nuts Nutrition 0.000 claims description 2
- 239000010815 organic waste Substances 0.000 claims description 2
- 239000011236 particulate material Substances 0.000 claims description 2
- 235000009566 rice Nutrition 0.000 claims description 2
- 239000010801 sewage sludge Substances 0.000 claims description 2
- 239000002002 slurry Substances 0.000 claims description 2
- 235000013616 tea Nutrition 0.000 claims description 2
- 239000002699 waste material Substances 0.000 claims description 2
- 241000207836 Olea <angiosperm> Species 0.000 claims 1
- 238000002425 crystallisation Methods 0.000 claims 1
- 230000005712 crystallization Effects 0.000 claims 1
- 238000003801 milling Methods 0.000 claims 1
- 235000012015 potatoes Nutrition 0.000 claims 1
- 240000007817 Olea europaea Species 0.000 description 1
- 230000003134 recirculating Effects 0.000 description 1
- 230000002087 whitening Effects 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Description
提供された実施形態の説明は代表例のみを示すものであり、特許請求の範囲により規定される発明の範囲を限定することを意図するものではない。
本発明の実施形態として、例えば以下を挙げることができる。
[1] ・熱い再循環粒子との接触により添加炭素質材料が熱分解される、第1の熱分解反応チャンバー（1）であって、炭素質材料のための入口（1a）、流動化ガスのための入口（1c）、第1の反応チャンバー（1）の上部にある、炭素含有チャー粒子及び再循環不活性粒子を担持する製品ガスのための出口（1b）、並びに、第一のチャーガス化チャンバー（5）からの製品ガスのための入口（1d）を有する、第1の熱分解反応チャンバー（1）、
・1又は複数のセパレーター（4）であって、第1の反応チャンバー（1）からの粒子を担持する製品ガスが受け入れられる入口（4a）、及び粒子がセパレーターを出て1又は複数の配管（14）を介して第一のチャーガス化チャンバー（5）に入るための出口（4b）を有する、セパレーター（4）、
・熱分解され及び再循環する粒子のための入口（5a）、第一のチャーガス化チャンバー（5）の下部にある流動化ガス（6）のための入口（5b）、第一のチャーガス化チャンバー（5）の上部にある生成ガスのための出口（5d）、及び第一のチャーガス化チャンバー（5）の下部にあり、粒子戻り配管（7）に開口する粒子のための出口（5c）を有する第一のチャーガス化チャンバー（5）であって、粒子戻り配管（7）が中間のチャーガス化チャンバー（9）に開口する、前記第一のチャーガス化チャンバー（5）、並びに
・第一のチャーガス化チャンバー（5）からの粒子のための入口（9a）及び反応器（9）の下部にある流動化ガス（例えばO 2 /H 2 Oを含むガス）のための入口（9b）を含み、さらに、チャンバー（9）の上部からの粒子を担持する生成ガスのための出口（9c）であって、第1の反応チャンバー（1）の下部につながる少なくとも1の出口を有し、かつ流動化ガスを第1の反応チャンバー（1）に供給する配管（8）に開口している出口（9c）も含む、中間のチャーガス化チャンバー（9）
を含む、添加炭素質材料の熱処理のための循環流動床（CFB）反応器。
[2] 中間のチャーガス化チャンバー（9）からの流動化ガスのための入口（1c）が、第一のチャーガス化チャンバー（5）からのガスのための入口（1d）の下方、すなわち上流側に位置する、[1]に記載のCFB反応器。
[3] 灰分のための出口が1若しくは複数のセパレーター（4）及び/又は中間のチャーガス化チャンバー（9）の底部に備えられている、[1]に記載のCFB反応器。
[4] 中間のチャーガス化反応器の断面積が第一のチャーガス化チャンバー（5）の断面積よりも少なくとも50％小さい、[1]に記載のCFB反応器。
[5] 中間のチャーガス化チャンバー（9）からの流動化ガスのための入口（1c）が、熱分解反応チャンバー（1）への炭素質材料のためのあらゆる入口（1a）の下方、すなわち上流側に位置する、[1]に記載のCFB反応器。
[6] 反応器が、
（a）中間のチャーガス化チャンバーの頂部が第一のチャーガス化チャンバーの頂部レベルと底部レベルとの中間レベルに位置し；
（b）中間のチャーガス化チャンバー（9）の頂部が第一のチャーガス化チャンバー（5）の流動化ガスの大部分が導入されるレベルよりも高いレベルに位置し；及び/又は
（c）中間のチャーガス化チャンバーの容積の50％よりも多くが第一のチャーガス化チャンバーの底部よりも下であり、熱分解チャンバーの底部よりも下のレベルに位置する
ように構成される、[1]に記載のCFB反応器。
[7] 作動中、粒子の第1の流動床（11）が第一のチャーガス化チャンバー（5）に提供され、前記第1の流動床（11）の体積が流動化ガスを流動床の底部に加えるレベルより上で同じ流動床の表面までに存在する体積として定義され、第1の流動床（11）の体積より上がガス及び同伴微粒子を含むより低い比重のフリーボード体積（13）である、[1]に記載のCFB反応器。
[8] 作動中、粒子が中間のチャーガス化チャンバー（9）を通って運ばれて粒子の第2の流動床（10）を形成し、この第2の流動床（10）の体積が流動化ガスを流動床の底部に加えるレベルより上で中間のチャーガス化チャンバーの上部にある生成ガス及び粒子のための出口（9c）の中心までの体積として定義され、中間のチャーガス化チャンバー（9）の第2の流動床（10）の高さ（h 10 ）が第一のチャーガス化チャンバー（5）の第1の流動床（11）の高さ（h 11 ）より高い、[1]に記載のCFB反応器。
[9] 作動中、粒子が中間のチャーガス化チャンバー（9）を通って運ばれて粒子の第2の流動床（10）を形成し、この第2の流動床（10）の体積が流動化ガスを流動床の底部に加えるレベルより上で中間のチャーガス化チャンバーの上部にある生成ガス及び粒子のための出口（9c）の中心までの体積として定義され、第一のチャーガス化チャンバー（5）の底部と頂部との間の圧力差が中間のチャーガス化チャンバー（9）の底部と頂部との間よりも小さい、[1]に記載のCFB反応器。
[10] 熱分解チャンバーの底部から15％以内に、流動化ガスを導入することができるノズルを更に含む、[1]に記載のCFB反応器。
[11] ・低いO 2 含有量を有する流動化ガス及び熱い不活性再循環粒子が流動し、温度T 1 が400〜850℃である第1の熱分解反応チャンバー中に炭素質材料を導入する第１の工程ステップであって、第1の工程ステップから部分的に変換された粒子（すなわちチャー）及び再循環床粒子を担持する製品ガスを生成する、第1の工程ステップ、
・第1のステップからの製品ガスを再循環及び部分的に変換されたチャー粒子から分離する第2の工程ステップであって、製品ガスが工程から出る一方で、分離されたチャー粒子及び床粒子が第3の工程ステップに入る、第2の工程ステップ、
・第一のチャー反応器において行われる第3の工程ステップであって、分離されたチャー中に残存する炭素質材料が流動床において600〜850℃の温度T 2 で分解酸化処理を受けて、第一のチャー反応器の上部から取り出される製品ガスを生成し、製品ガスが同伴微粒子の一部と一緒に第1の工程ステップに入る一方で、第一のチャー反応器の下部からの床粒子が第4の工程ステップに運ばれる、第3の工程ステップ、並びに
・残存するチャーが流動床において600〜850℃の温度T 3 で第2の分解酸化処理を受ける第4の工程ステップであって、再循環粒子と一緒に第4のステップを出て、流動化ガスとして第1の工程ステップに入る製品ガスを生成する、第4の工程ステップ、
を含む、炭素質材料から望ましい発熱量を有する製品ガスを製造する方法であって、
第4の工程ステップの流動床におけるガス滞留時間（t 10 ）が、第3の工程ステップの流動床におけるガス滞留時間（t 11 ）よりも長い（t 10 ＞t 11 ）、方法。
[12] （a）t 10 が＞1.2t 11 、好適には＞1.5t 11 であり；
（b）第3の工程ステップの温度T 2 と第4の工程ステップの温度T 3 とが10℃未満で異なり、すなわちT 3 -T 2 ＜10℃、通常T 3 -T 2 ＜5℃であり；
（c）温度T 1 が400〜800℃、通常625〜775℃であり；及び/又は
（d）温度T 2 が650〜800℃、通常700〜800℃である、
[11]に記載の方法。
[13] 第1の工程ステップの温度が、第1の工程ステップへの流動化ガス及び再循環粒子の流れを決定する第4の工程ステップへの流動化ガスの流れを調節することにより制御される、[11]に記載の方法。
[14] 第3の工程ステップにおける床材料の少なくとも95重量％が不活性粒子材料である一方で、材料の5重量％未満が残存する炭素質材料である、[11]に記載の方法。
[15] 炭素質材料が任意の1又は複数の、穀物わら、稲わら、関連穀粒精白廃棄物流；別の作物、例えばサトウキビ、モロコシ、テンサイ、トウモロコシ、ジャガイモ、ナッツ、茶、綿、ワイン、オリーブ及びアブラヤシの残渣；例えば海藻を含む藻類；例えばミスカンツス（Miscantus）を含む草類を含むエネルギー作物；ヤナギ及びポプラを含む早生樹に基づく短期循環森林穀物からの残渣；例えば塩を含む水の近くでの成長により又はその他塩を含む水との接触により高濃度の塩を有する作物；肉及び骨粉を含む肉製品産業からの残渣；脱水糞尿スラリーを含む家畜糞尿；このようなストリームに由来する有機分を含む都市及び産業有機廃棄物；下水汚泥；又は木材の加工による繊維及びリグニン製品などのエネルギーを含む残渣並びに精製していない有機製品を含む、[11]に記載の方法。
[16] 作動中、第一のチャーガス化チャンバー（5）の底部と頂部との間の圧力差が中間のチャーガス化チャンバー（9）の底部と頂部との間よりも小さい、[11]に記載の方法。
The description of the provided embodiments is merely representative and is not intended to limit the scope of the invention as defined by the claims.
Examples of the present invention include the following.
[1] A first pyrolysis reaction chamber (1) in which the added carbonaceous material is pyrolyzed by contact with hot recirculating particles, the inlet for the carbonaceous material (1a), fluidized gas Inlet (1c) for gas, outlet (1b) for product gas carrying carbon-containing char particles and recycle inert particles at the top of the first reaction chamber (1), and first char gas A first pyrolysis reaction chamber (1), having an inlet (1d) for product gas from the gasification chamber (5),
One or more separators (4), the inlet (4a) for receiving the product gas carrying the particles from the first reaction chamber (1), and one or more pipes (the particles exit the separators) 14) a separator (4), having an outlet (4b) for entering the first char gasification chamber (5) via
Inlet (5a) for pyrolyzed and recirculated particles, inlet (5b) for fluidizing gas (6) at the bottom of the first char gasification chamber (5), first char gasification chamber The outlet (5d) for the product gas at the top of (5) and the outlet (5c) for the particles at the bottom of the first char gasification chamber (5) and open to the particle return pipe (7) A first char gasification chamber (5) having a particle return line (7) opening into an intermediate char gasification chamber (9); and
The inlet (9a) for the particles from the first char gasification chamber (5) and the inlet for the fluidizing gas (eg gas containing O 2 / H 2 O ) at the bottom of the reactor (9) ( 9b) and further comprising an outlet (9c) for the product gas carrying particles from the upper part of the chamber (9), which has at least one outlet leading to the lower part of the first reaction chamber (1) And an intermediate char gasification chamber (9) that also includes an outlet (9c) that opens into a pipe (8) that supplies fluidizing gas to the first reaction chamber (1)
A circulating fluidized bed (CFB) reactor for heat treatment of added carbonaceous materials.
[2] The inlet (1c) for fluidizing gas from the intermediate char gasification chamber (9) is below, ie upstream from, the inlet (1d) for gas from the first char gasification chamber (5) The CFB reactor according to [1], which is located in
[3] The CFB reactor according to [1], wherein an outlet for ash is provided at the bottom of one or more separators (4) and / or an intermediate char gasification chamber (9).
[4] The CFB reactor according to [1], wherein the cross-sectional area of the intermediate char gasification reactor is at least 50% smaller than the cross-sectional area of the first char gasification chamber (5).
[5] The inlet (1c) for fluidizing gas from the intermediate char gasification chamber (9) is below, ie upstream of any inlet (1a) for carbonaceous material to the pyrolysis reaction chamber (1) The CFB reactor according to [1], which is located on the side.
[6] The reactor is
(A) the top of the intermediate char gasification chamber is located at an intermediate level between the top level and the bottom level of the first char gasification chamber;
(B) the top of the intermediate char gasification chamber (9) is located at a level higher than the level at which most of the fluidizing gas in the first char gasification chamber (5) is introduced; and / or
(C) More than 50% of the volume of the intermediate char gasification chamber is below the bottom of the first char gasification chamber and is located at a level below the bottom of the pyrolysis chamber
The CFB reactor according to [1], which is configured as follows.
[7] In operation, a first fluidized bed (11) of particles is provided to a first char gasification chamber (5), the volume of the first fluidized bed (11) passing the fluidized gas to the bottom of the fluidized bed. Defined as the volume that exists above the level added to the surface of the same fluidized bed and above the volume of the first fluidized bed (11) is the lower specific gravity freeboard volume (13) containing gas and entrained particulates The CFB reactor according to [1].
[8] During operation, the particles are transported through an intermediate char gasification chamber (9) to form a second fluidized bed (10) of particles, and the volume of this second fluidized bed (10) is fluidized Defined as the volume to the center of the outlet (9c) for product gas and particles above the level at which the gas is added to the bottom of the fluidized bed and at the top of the intermediate char gasification chamber, of the intermediate char gasification chamber (9) The height (h 10 ) of the second fluidized bed (10) is higher than the height (h 11 ) of the first fluidized bed (11) of the first char gasification chamber (5). CFB reactor.
[9] During operation, the particles are transported through an intermediate char gasification chamber (9) to form a second fluidized bed (10) of particles, and the volume of this second fluidized bed (10) is fluidized The first char gasification chamber (5) is defined as the volume to the center of the outlet (9c) for the product gas and particles above the level at which gas is added to the bottom of the fluidized bed and at the top of the intermediate char gasification chamber The CFB reactor according to [1], wherein the pressure difference between the bottom and the top of the middle is smaller than between the bottom and the top of the intermediate char gasification chamber (9).
[10] The CFB reactor according to [1], further including a nozzle capable of introducing a fluidizing gas within 15% from the bottom of the pyrolysis chamber.
[11] Introducing carbonaceous material into the first pyrolysis reaction chamber in which fluidized gas with low O 2 content and hot inert recycle particles flow and temperature T 1 is 400-850 ° C. A first process step that produces a product gas carrying particles (ie char) and recirculated bed particles partially converted from the first process step;
A second process step that separates the product gas from the first step from the recirculated and partially converted char particles, wherein the product gas exits the process while separated char particles and bed particles Enters the third process step, the second process step,
A third process step performed in the first char reactor, wherein the carbonaceous material remaining in the separated char is subjected to a cracking oxidation treatment at a temperature T 2 of 600 to 850 ° C. in the fluidized bed ; Producing a product gas that is withdrawn from the top of the first char reactor and the product gas enters the first process step along with some of the entrained particulates, while the bed particles from the bottom of the first char reactor Is carried to the fourth process step, the third process step, and
A fourth process step in which the remaining char undergoes a second cracking oxidation treatment at a temperature T 3 of 600-850 ° C. in the fluidized bed, leaving the fourth step together with the recirculated particles and fluidizing Generating a product gas that enters the first process step as a gas, a fourth process step;
A method for producing a product gas having a desired calorific value from a carbonaceous material, comprising:
The method wherein the gas residence time (t 10 ) in the fluidized bed of the fourth process step is longer than the gas residence time (t 11 ) in the fluidized bed of the third process step (t 10 > t 11 ).
[12] (a) t 10 > 1.2 t 11 , preferably> 1.5 t 11 ;
(B) The temperature T 2 of the third process step and the temperature T 3 of the fourth process step differ by less than 10 ° C., ie T 3 -T 2 <10 ° C., usually T 3 -T 2 <5 ° C. Yes;
(C) the temperature T 1 is 400-800 ° C, usually 625-775 ° C; and / or
(D) temperature T 2 is 650 to 800 ° C., usually 700 to 800 ° C.,
The method according to [11].
[13] The temperature of the first process step is controlled by adjusting the flow of fluidizing gas to the fourth process step that determines the flow of fluidizing gas and recirculated particles to the first process step. The method according to [11].
[14] The method according to [11], wherein at least 95% by weight of the floor material in the third process step is an inert particulate material, while less than 5% by weight of the material is a remaining carbonaceous material.
[15] Grain straw, rice straw, related grain whitening waste logistics; any other crop such as sugar cane, sorghum, sugar beet, corn, potato, nuts, tea, cotton, wine, any one or more carbonaceous materials Olive and oil palm residues; eg algae including seaweeds; energy crops including grasses including eg Miscantus; residues from short-circulating forest crops based on fast-growing trees including willows and poplars; eg near salty water Crops with high concentrations of salt by growing on or in contact with water containing other salts; residues from the meat products industry including meat and bone meal; livestock manure containing dehydrated manure slurries; organics from such streams Municipal and industrial organic waste containing sewage sludge; or residues containing energy such as fiber and lignin products from the processing of wood and refined Including organic products not, The method according to [11].
[16] As described in [11], in operation, the pressure difference between the bottom and top of the first char gasification chamber (5) is smaller than between the bottom and top of the intermediate char gasification chamber (9) the method of.
Claims (21)
・1又は複数のセパレーター（4）であって、第1の反応チャンバー（1）からの粒子を担持する製品ガスが受け入れられる入口（4a）、及び粒子がセパレーターを出て1又は複数の配管（14）を介して第一のチャーガス化チャンバー（5）に入るための出口（4b）を有する、セパレーター（4）、
・熱分解され及び再循環する粒子のための入口（5a）、第一のチャーガス化チャンバー（5）の下部にある流動化ガス（6）のための入口（5b）、第一のチャーガス化チャンバー（5）の上部にある生成ガスのための出口（5d）、及び第一のチャーガス化チャンバー（5）の下部にあり、粒子戻り配管（7）に開口する粒子のための出口（5c）を有する第一のチャーガス化チャンバー（5）であって、粒子戻り配管（7）が中間のチャーガス化チャンバー（9）に開口する、前記第一のチャーガス化チャンバー（5）、並びに
・第一のチャーガス化チャンバー（5）からの粒子のための入口（9a）及び反応器（9）の下部にある流動化ガス（例えばO2/H2Oを含むガス）のための入口（9b）を含み、さらに、チャンバー（9）の上部からの粒子を担持する生成ガスのための出口（9c）であって、第1の反応チャンバー（1）の下部につながる少なくとも1の出口を有し、かつ流動化ガスを第1の反応チャンバー（1）に供給する配管（8）に開口している出口（9c）も含む、中間のチャーガス化チャンバー（9）
を含む、添加炭素質材料の熱処理のための循環流動床（CFB）反応器。 A first pyrolysis reaction chamber (1) in which the added carbonaceous material is pyrolyzed by contact with hot recycled particles, the inlet for the carbonaceous material (1a), for the fluidized gas An inlet (1c), an outlet (1b) for the product gas carrying carbon-containing char particles and recycle inert particles at the top of the first reaction chamber (1), and a first char gasification chamber ( 5) a first pyrolysis reaction chamber (1), having an inlet (1d) for product gas from
One or more separators (4), the inlet (4a) for receiving the product gas carrying the particles from the first reaction chamber (1), and one or more pipes (the particles exit the separators) 14) a separator (4), having an outlet (4b) for entering the first char gasification chamber (5) via
Inlet (5a) for pyrolyzed and recirculated particles, inlet (5b) for fluidizing gas (6) at the bottom of the first char gasification chamber (5), first char gasification chamber The outlet (5d) for the product gas at the top of (5) and the outlet (5c) for the particles at the bottom of the first char gasification chamber (5) and open to the particle return pipe (7) A first char gasification chamber (5), wherein the particle return pipe (7) opens into an intermediate char gasification chamber (9), and the first char gasification chamber (5) An inlet (9a) for particles from the crystallization chamber (5) and an inlet (9b) for a fluidizing gas (eg a gas containing O 2 / H 2 O) at the bottom of the reactor (9); In addition, the product gas carrying particles from the top of the chamber (9) An outlet (9c) having at least one outlet connected to a lower portion of the first reaction chamber (1) and supplying fluidizing gas to the first reaction chamber (1) (8) Intermediate char gasification chamber (9), including outlet (9c) opening in
A circulating fluidized bed (CFB) reactor for heat treatment of added carbonaceous materials.
・第1のステップからの製品ガスを再循環及び部分的に変換されたチャー粒子から分離する第2の工程ステップであって、製品ガスが工程から出る一方で、分離されたチャー粒子及び床粒子が第3の工程ステップに入る、第2の工程ステップ、
・第一のチャー反応器において行われる第3の工程ステップであって、分離されたチャー中に残存する炭素質材料が流動床において600〜850℃の温度T2で分解酸化処理を受けて、第一のチャー反応器の上部から取り出される製品ガスを生成し、製品ガスが同伴微粒子の一部と一緒に第1の工程ステップに入る一方で、第一のチャー反応器の下部からの床粒子が第4の工程ステップに運ばれる、第3の工程ステップ、並びに
・残存するチャーが流動床において600〜850℃の温度T3で第2の分解酸化処理を受ける第4の工程ステップであって、再循環粒子と一緒に第4のステップを出て、流動化ガスとして第1の工程ステップに入る製品ガスを生成する、第4の工程ステップ、
を含む、炭素質材料から望ましい発熱量を有する製品ガスを製造する方法であって、
第4の工程ステップの流動床におけるガス滞留時間（t10）が、第3の工程ステップの流動床におけるガス滞留時間（t11）よりも長い（t10＞t11）、方法。 A first introducing a carbonaceous material into a first pyrolysis reaction chamber in which a fluidized gas having a low O 2 content and hot inert recycle particles flow and a temperature T 1 of 400-850 ° C. A first process step that produces a product gas carrying particles (ie char) and recirculated bed particles partially converted from the first process step,
A second process step that separates the product gas from the first step from the recirculated and partially converted char particles, wherein the product gas exits the process while separated char particles and bed particles Enters the third process step, the second process step,
A third process step performed in the first char reactor, wherein the carbonaceous material remaining in the separated char is subjected to a cracking oxidation treatment at a temperature T 2 of 600 to 850 ° C. in the fluidized bed; Producing a product gas that is withdrawn from the top of the first char reactor and the product gas enters the first process step along with some of the entrained particulates, while the bed particles from the bottom of the first char reactor Is transferred to a fourth process step, and a third process step, and a fourth process step in which the remaining char undergoes a second cracking oxidation treatment at a temperature T 3 of 600-850 ° C. in a fluidized bed. A fourth process step, producing a product gas that exits the fourth step together with the recirculated particles and enters the first process step as a fluidizing gas;
A method for producing a product gas having a desired calorific value from a carbonaceous material, comprising:
The method wherein the gas residence time (t 10 ) in the fluidized bed of the fourth process step is longer than the gas residence time (t 11 ) in the fluidized bed of the third process step (t 10 > t 11 ).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DKPA201270432 | 2012-07-17 | ||
| DKPA201270432 | 2012-07-17 | ||
| PCT/DK2013/050242 WO2014012556A1 (en) | 2012-07-17 | 2013-07-17 | Apparatus and methods for gasification |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| JP2015522106A JP2015522106A (en) | 2015-08-03 |
| JP2015522106A5 true JP2015522106A5 (en) | 2016-08-18 |
| JP6195923B2 JP6195923B2 (en) | 2017-09-13 |
Family
ID=48874739
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2015521981A Expired - Fee Related JP6195923B2 (en) | 2012-07-17 | 2013-07-17 | Apparatus and method for gasification |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20150218456A1 (en) |
| EP (1) | EP2875104A1 (en) |
| JP (1) | JP6195923B2 (en) |
| CN (1) | CN104704088B (en) |
| IN (1) | IN2014DN11229A (en) |
| WO (1) | WO2014012556A1 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9566546B2 (en) * | 2014-01-21 | 2017-02-14 | Saudi Arabian Oil Company | Sour gas combustion using in-situ oxygen production and chemical looping combustion |
| JP7182542B2 (en) * | 2016-11-16 | 2022-12-02 | アトキンス エナジー グローバル ソリューションズ エルエルシー | Volume reduction of radioactive waste due to heat |
| CN110791326B (en) * | 2019-11-21 | 2021-10-12 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method |
| CN112852498B (en) * | 2020-12-30 | 2022-03-04 | 中国科学院工程热物理研究所 | Fuel dealkalization device and method, circulating fluidized bed gasification device and method |
| IT202200011075A1 (en) * | 2022-05-26 | 2023-11-26 | Viemme Impianti S R L | PROCESS FOR THE DISPOSAL OF OLIVE POMAE |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2563118B1 (en) * | 1984-04-20 | 1987-04-30 | Creusot Loire | PROCESS AND PLANT FOR TREATING FLUIDIZED BED MATERIAL |
| FI20055237L (en) * | 2005-05-18 | 2006-11-19 | Foster Wheeler Energia Oy | Method and apparatus for gasification of carbonaceous material |
| JP4835581B2 (en) * | 2007-11-14 | 2011-12-14 | 株式会社Ｉｈｉ | Circulating fluidized bed reformer |
| JP5282465B2 (en) * | 2008-07-11 | 2013-09-04 | 株式会社Ｉｈｉ | Method and apparatus for controlling fluid medium residence time of fluidized bed gasifier in gasification facility |
| CN101781583B (en) * | 2009-01-21 | 2014-02-26 | 中国科学院过程工程研究所 | Method and device for utilizing high value through pyrolysis and gasification of coal |
| JP5532207B2 (en) * | 2009-02-20 | 2014-06-25 | 独立行政法人産業技術総合研究所 | Circulating fluidized bed gasification reactor |
| AT509586B8 (en) * | 2010-06-11 | 2011-12-15 | Univ Wien Tech | IMPROVED SWITCH LAYER REACTOR SYSTEM |
| CN101921627B (en) * | 2010-07-30 | 2013-03-13 | 陕西华祥能源科技集团有限公司 | Air-oil co-production device forcoupling fluidized bed pulverized coal gasification and solid heat carrier pyrolysis and method therefor |
| CN102277200A (en) * | 2011-07-05 | 2011-12-14 | 舒克孝 | Method for preparing coal gas by virtue of pulverized coal grading gasification |
-
2013
- 2013-07-17 WO PCT/DK2013/050242 patent/WO2014012556A1/en active Application Filing
- 2013-07-17 US US14/415,062 patent/US20150218456A1/en not_active Abandoned
- 2013-07-17 EP EP13741667.3A patent/EP2875104A1/en not_active Withdrawn
- 2013-07-17 IN IN11229DEN2014 patent/IN2014DN11229A/en unknown
- 2013-07-17 JP JP2015521981A patent/JP6195923B2/en not_active Expired - Fee Related
- 2013-07-17 CN CN201380038048.5A patent/CN104704088B/en not_active Expired - Fee Related
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Qureshi et al. | A technical review on semi-continuous and continuous pyrolysis process of biomass to bio-oil | |
| JP2015522106A5 (en) | ||
| CN107708868B (en) | Improved catalysis rapid pyrolysis method with impurity removal | |
| JP6281802B2 (en) | Method and apparatus for solid-liquid mixture processing | |
| JP7234241B2 (en) | Method for preparing char product and syngas mixture | |
| EP3514109B1 (en) | Hydropyrolysis of biomass-containing feedstocks | |
| KR101371884B1 (en) | Method for producing solid fuel using biomass material and the solid fuel therefrom | |
| CA2575910A1 (en) | Biomass thermal oiling | |
| US20200181500A1 (en) | Use of cooling media in biomass conversion process | |
| JP6195923B2 (en) | Apparatus and method for gasification | |
| NL2019553B1 (en) | Process to prepare an activated carbon product and a syngas mixture | |
| MX2014008176A (en) | Two-stage reactor and process for conversion of solid biomass material. | |
| CN112469802B (en) | Biomass injection in fluidized bed catalytic pyrolysis reactor | |
| NL2016437B1 (en) | Process to prepare a char product and a syngas mixture. | |
| WO1994024228A1 (en) | Process for the production of liquid fuel, gaseous fuel, coke and active coal | |
| US20150225650A1 (en) | Biomass feed system including gas assist | |
| US9862901B2 (en) | Apparatus and methods for gasification | |
| US20140318944A1 (en) | Catalytic pyrolysis of biomass using a multi-stage catalyst regenerator | |
| KR20060060793A (en) | Recyling of food waste by rapid pyrolysis process | |
| US20230151281A1 (en) | Process to prepare a gas oil product | |
| KR101611486B1 (en) | Method for fast pyrolysis of biomass using double tube type fluidized bed reactor | |
| WO2024094285A1 (en) | Methods for providing pyrolysis oil from holocellulose and lignin comprising biomass | |
| WO2023088881A1 (en) | Process to continuously prepare a gas oil product |