JP5384649B2 - 炭素質フィードストックのガス化のための方法 - Google Patents
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Description
本出願は、米国特許法119条のもと、米国仮出願番号 61/098、477(出願日2008年9月19日)(これの開示はあたかも十分に記載しているかのようにする全ての目的で、参照により本明細書に組み入れられる)からの優先権を主張する。
(a)炭素質フィードストック、酸素リッチガス流、アルカリ金属ガス化触媒、及びスチームを触媒ガス化装置に供給する;
(b)炭素質フィードストックを、触媒ガス化装置中、スチーム、酸素リッチガス流、及びアルカリ金属ガス化触媒の存在下、且つ適した温度及び圧力下で反応させて、メタン、二酸化炭素、水素、一酸化炭素、及び硫化水素を含む複数のガス生成物を含む、第1のガス流を形成させる;
(c)場合により、第1のガス流に存在する少なくとも一酸化炭素の一部及び少なくとも水素の一部を、触媒メタネーター中、耐硫黄性メタン化触媒の存在下反応させて、第1のメタン富化したガス流を生成させる;
(d)第1のガス流(又は存在する場合、第1のメタン富化ガス流)から二酸化炭素の大部分及び硫化水素の大部分を除去して、第1のガス流(又は存在する場合、第1のメタン富化ガス流)からメタンの大部分を含む第2のガス流を生成させる;
(e)場合により、第2のガス流が水素及び約100ppmより大の一酸化炭素を含む場合、第2のガス流中に存在する一酸化炭素及び水素を、触媒メタネーター中、メタン化触媒の存在下反応させて、第2のメタン富化ガス流を生成させる;及び
(f)第2のガス流(又は存在する場合、第2のメタン富化ガス流)を回収する、
ここにおいて、(i)工程(c)及び工程(e)の少なくとも1つが存在し、(ii)第2のガス流(又は存在する場合、第2のメタン富化ガス流)がメタン生成物流であるか、又は第2のガス流(又は存在する場合、第2のメタン富化ガス流)が精製され、メタン生成物流を発生させる。
(a)炭素質フィードストック、酸素リッチガス流、アルカリ金属ガス化触媒、及びスチームを連続的に触媒ガス化装置に供給する;
(b)炭素質フィードストックを、触媒ガス化装置中、スチーム、酸素リッチガス流、及びアルカリ金属ガス化触媒の存在下、且つ適した温度及び圧力下で連続的に反応させて、メタン、二酸化炭素、水素、一酸化炭素、及び硫化水素を含む複数のガス生成物を含む、第1のガス流を形成させる;
(c)場合により、第1のガス流中に存在する少なくとも一酸化炭素の一部及び少なくとも水素の一部を、触媒メタネーター中、耐硫黄性触媒の存在下反応させて、第1のメタン富化ガス流を生成させる;
(d)第1のガス流(又は存在する場合、第1のメタン富化ガス流)から二酸化炭素の大部分及び硫化水素の大部分を連続的に除去して、第1のガス流(又は存在する場合、第1のメタン富化ガス流)からメタンの大部分を含む第2のガス流を生成させる;
(e)場合により、第2のガス流が水素及び約100ppmより大の一酸化炭素を含む場合、触媒メタネーター中、メタン化触媒の存在下、第2のガス流中の一酸化炭素と水素を反応させて、第2のメタン富化ガス流を生成させる;及び、
(f)第2のガス流(又は存在する場合、第2のメタン富化ガス流)を連続的に回収する、
ここにおいて、(i)工程(c)及び工程(e)の少なくとも1つが存在し、(ii)第2のガス流(又は存在する場合、第2のメタン富化ガス流)がメタン生成物流である、又は第2のガス流(又は存在する場合、第2のメタン富化ガス流)が精製され、メタン生成物流を発生させる。
本開示は、炭素質フィードストックを、少なくとも、メタンを含む複数のガス生成物に転換するプロセスに関し、そのプロセスは、他の工程の中でも特に、炭素質フィードストック、酸素リッチガス流、アルカリ金属ガス化触媒、及び、スチームを触媒ガス化装置に提供して、炭素質フィードストックを、アルカリ金属触媒、及び、酸素リッチガス流の存在のもと、複数のガス生成物に転換することを含んでいる。特に、本発明は改良された「ワンススルー(once−through)」ガス化方法を提供するものであり、「ワンススルー」とは、本明細書にて使用されている様に、好都合なことに一酸化炭素、又は、水素を触媒ガス化装置への再循環の必要がないことを意味する。本プロセスの一酸化炭素と水素の必要量は、触媒ガス化装置内の酸素リッチガス流の存在のもと、炭素質フィードストックの部分燃焼によって、そのまま(in situ)実質的に満たすことができる。
とができる。
は、本明細書において他に規定されていない限り、言及された材料の約90%より多いこと、好ましくは言及された物質の95%より多いこと、及び、より好ましくは言及された物質の97%より多いことを意味する。百分率は、分子(メタン、二酸化炭素、一酸化炭素、及び、硫化水素など)について言及がなされているときは、モル基準であり、他の場合には重量基準である(同伴炭素質微粉など)。
本発明の一実施態様において、図1に示されている様に、メタン生成物流(80)を、触媒化炭素質フィードストック(30)から生成することができる。メタン、一酸化炭素、水素、二酸化炭素、及び、硫化水素を含む、第1のガス流(40)を生成するために、スチーム源(500)からのスチーム(51)、酸素源(900)からの酸素リッチガス流(91)(精製酸素など))、及び、触媒化炭素質フィードストック(30)を触媒ガス化装置(300)に供給することができる。触媒ガス化装置に供給されるスチームを要求の温度と圧力に過熱するために、プロセスの数多い段階の1つによって熱回収を用いることができ、その結果、独立した過熱器の必要が無い。
炭素に蒸気を当てる: C + H2O → CO + H2 (I)
水−ガスのシフト: CO + H2O → H2 + CO2 (II)
COのメタン化: CO+3H2 → CH4 + H2O (III)
以下に、より詳しく記述されている様に、本発明の一実施態様において、ガス化触媒はアルカリ金属ガス化触媒を含むことができる。
(a)炭素質材料の処理
バイオマス、及び、非バイオマス(上記を参照)等の炭素質材料は、1つ又はそれ以上の炭素質微粒子を産出するための、衝撃破砕、及び、湿式又は乾式粉砕等の、当業者に知られている如何なる方法によっても、別々に又は一緒に、破砕、及び/又は、粉砕によって、製造することができる。炭素質材料源の破砕、及び/又は、粉砕に用いられるプロセス次第で、得られる炭素質微粒子は、触媒化炭素質フィードストックを形成するために、触媒ローディング・プロセスにて使用するための、加工原料を提供するために、大きさによって分けてもよい(即ち、大きさに従って分離される)。
1つ又はそれ以上の炭素質微粒子は、少なくとも1つのアルカリ金属源を典型的に含む、少なくとも1つのガス化触媒を会合させるために、さらに処理されて、触媒化炭素質フィードストック(30)を発生する。
(a)触媒回収
記述された条件下での触媒化炭素質フィードストック(30)の反応により、触媒ガス化装置から、第1のガス流(40)と固形炭化生成物が、一般的にもたらされる。固形炭化生成物は、一般的に、多量の未反応炭素質材料と同伴触媒を含んでいる。固形炭化生成物は、サンプリング、ガス抜き、及び/又は、チャー出口からの触媒回収のために、反応室から除去することができる。
生成物の精製は、例えば、任意の微量夾雑物除去、アンモニア除去、及び、回収、並びに、サワーシフト・プロセスを含んでもよい。酸性ガス除去(上記参照)は、熱交換器から直接送られた冷却された第1のガス流(50)に、又は、(i)1つまたはそれ以上の、微量成分除去ユニット;(ii)1つまたはそれ以上の、サワーシフト・ユニット;(iii)1つまたはそれ以上の、アンモニア除去ユニット、及び、(iv)硫黄に対する耐性のある触媒メタネーターの、1つまたはそれ以上を通って来た冷却された第1のガス流に、実施されてよい。
当業者には良く知られているように、ガス流の、例えば、冷却された第1のガス流(50)の混入物のレベルは、触媒化炭素質フィードストックを製造するための、炭素質材料の特性次第である。例えば、Illinois ♯6のような、ある種の石炭は、硫黄含有量が高く、高COS混入物をもたらすことがあり;Powder River Basinのような、他の石炭は、触媒ガス化装置内で揮発することができるかなり高いレベルの水銀を含むことがある。
ガス流、例えば、冷却された第1のガス流(50)には、COの一部をCO2に変え、H2の割合を増やすために、水性媒体(スチームのような)の存在のもと、水−ガス・シフト反応を施すことができる。ある実施例においては、水素の割合増加の発生を、以下に述べる様に、メタンから分離することができる、水素生成物ガスの形成に使用することができる。ある、他の実施例では、サワーシフト・プロセスを、次のメタネーターに供給するために、ガス流、例えば、冷却された第1のガス流(50)中の一酸化炭素対水素の割合を調整するために使用してもよい。水−ガス・シフト処理は、熱交換器から直接流れて来た冷却された第1のガス流に、又は、微量夾雑物除去ユニットを通過した、冷却された第1のガス流に行われてもよい。
当業者に良く知られているように、バイオマスのガス化、及び/又は、触媒ガス化装置のために酸素源として空気を利用することにより、生成物ガス流中に、かなりの量のアンモニアを製造することができる。場合により、ガス流、例えば、冷却された第1のガス流(50)を、アンモニアを回収するために、1つまたはそれ以上の、アンモニア回収ユニットにおいて、水によるスクラビングすることができる。アンモニア回収処理は、例えば、熱交換器から直接流れて来た、冷却された第2のガス流に、又は、(i)1つ又はそれ以上の微量夾雑物除去ユニット;及び、(ii)1つ又はそれ以上のサワーシフト・ユニットの、1つ又は双方から流れて来たガス流、例えば、冷却された第1のガス流(50)に実施されることがある。
第2のガス流、又は第2のメタン富化ガス流は、必要なときには、限定されるものではないが、低温蒸留、及び、モレキュラー・シーブ、又は、ガス分離膜(例えば、セラミック)の使用等の、当業者に知られている、いかなる適切なガス分離プロセスによっても、CH4を分離し取出すために、処理することができる。例えば、サワーシフト・プロセスが存在するときには、第2のガス流は、低温蒸留などの当業者に良く知られているプロセスにしたがって、分離することができる、メタンと水素を含むことがある。
スチーム源(500)によって生成されたスチームの一部は、プラント内にて使用し得る、又は、電力供給網に売却することができる電力を生産するために、スチームタービン等の、1つ又はそれ以上の発電機に供給されてもよい。ガス化方法内にて生産された高温・高圧のスチームを、電力の発生のために、スチームタービンに供給してもよい。例えば、第1のガス流(40)との接触で、熱交換器にてとらえられた熱エネルギーは、スチームタービンへ供給されるスチームの発生用に使用することができる。
当業者に知られたいずれかのプロセスに従い、プラント内の回収水の再循環、及び/又は、プラント・プロセスからの排水の廃棄を可能にするために、微量夾雑物除去、サワーシフト、アンモニア除去、及び/又は、触媒回収プロセスの、いずれか1つ又はそれ以上から生じる排水中の残余夾雑物を、排水処理ユニットにおいて、除去することができる。かかる残余夾雑物は、例えば、フェノール類、CO、CO2、H2S、COS、アンモニア、及び、水銀を含むことがある。例えば、H2S及びHCNは、排水のpHを約3の酸性とし、酸性排水をストリッピング塔において、イナート・ガスで処理し、アンモニアを除去するために、pHを約10に上げ、排水をイナート・ガスで、2度目の処理をすることにより、除去することができる(US5236557参照)。H2Sは、H2Sを浮遊選鉱又は濾過により除去し得る不溶性硫酸塩に転換するために、残余コークス微粒子の存在の下、酸化剤で排水を処理することにより除去することができる(US4478425参照)。フェノール類は、排水を、一価、及び、二価の塩基無機化合物を含む炭素質チャー(例えば、固形チャー生成物、又は、触媒回収後の除かれたチャー、上記を参照)と排水を接触させ、pHを調整することにより除去することができる(US4113615参照)。フェノール類はまた、有機溶剤で抽出し、次に、ストリッピング塔での排水処理により、除去することもできる(US3972693、US4025423、及び、US4162902参照)。
本発明のプロセスにおいて、各プロセスは、1つまたはそれ以上の、処理ユニット内で実行することができる。例えば、1つまたはそれ以上の、触媒ガス化装置には、1つまたはそれ以上の、触媒ローディングからの、及び/又は、フィードストック製造ユニット操作からの、炭素質フィードストックを供給することができる。同様に、1つまたはそれ以上の、触媒ガス化装置によって生成された第1のガス流を、例えば、既に組み入れられている米国特許出願番号12/492,467、12/492,477、12/492,484、12/492,489、及び12/492,497に述べられている様に、特定のシステム構成に応じて、別々に、又は、熱交換器、耐硫黄触媒メタネーター、酸性ガス除去ユニット、トリム・メタネーター、及び/若しくは、メタン取出しユニットの組合せによって、処理、又は、精製することができる。
本発明方法の一実施態様が図3に図示されている。ここにおいて、炭素質フィードストック(10)はフィードストック処理ユニット(100)に供給され、約2500μmより小さい平均粒子径を有する炭素質微粒子(20)に変換される。炭素質微粒子(20)は、触媒ローディング・ユニット(200)に供給され、ここで粒子をローディング・タンク中ガス化触媒を含む溶液と接触させ、過剰な水を濾過によって除去し、得られた湿ったケーキを乾燥機で乾燥して、触媒化炭素質フィードストック(30)を得る。触媒化炭素質フィードストックは触媒ガス化装置(300)に供給される。
本発明方法の別の実施態様が図4に図示されている。ここにおいて、炭素質フィードストック(10)はフィードストック処理ユニット(100)に供給され、約2500μmより小さい平均粒子径を有する炭素質微粒子(20)に変換される。炭素質微粒子(20)は触媒ローディング・ユニット(200)に送られ、ここで粒子をローディング・タンク中ガス化触媒を含む溶液と接触させ、過剰な水を濾過によって除去し、そして得られた湿ったケーキを乾燥機で乾燥して、触媒化炭素質フィードストック(30)を得る。触媒化炭素質フィードストックは触媒ガス化装置(300)に供給される。
Claims (11)
- 炭素質フィードストックから複数のガス生成物を生成させ、メタン生成物流を回収するための方法であって、
(a)炭素質フィードストック、酸素リッチガス流、アルカリ金属ガス化触媒、及びスチームを、触媒ガス化装置に供給する工程;
(b)炭素質フィードストックを、触媒ガス化装置中、スチーム、水素、一酸化炭素、酸素リッチガス流、及びアルカリ金属ガス化触媒の存在下、450℃から800℃の温度及び400psig(2859kPa絶対圧力)から1000psig(6996kPa絶対圧力)の圧力下で反応させて、メタン、二酸化炭素、水素、一酸化炭素、及び硫化水素を含む複数のガス生成物を含む第1のガス流を形成させる工程、ここで前記第1のガス流は、第1のガス流中のメタン、二酸化炭素、一酸化炭素、及び水素のモルに基づいて、少なくとも50mol%のメタン+二酸化炭素を含み;
(c)場合により、第1のガス流に存在する少なくとも一酸化炭素の一部及び少なくとも水素の一部を、触媒メタネーター中、耐硫黄性メタン化触媒の存在下反応させて、第1のメタン富化ガス流を生成させる工程;
(d)第1のガス流(又は存在する場合第1のメタン富化ガス流)から二酸化炭素の大部分及び硫化水素の大部分を除去して、第1のガス流(又は存在する場合第1のメタン富化ガス流)からメタンの大部分を含む第2のガス流を生成させる工程;
(e)場合により、第2のガス流が水素及び100ppmより大の一酸化炭素を含む場合、第2のガス流中に存在する一酸化炭素及び水素を、触媒メタネーター中、メタン化触媒の存在下反応させて、第2のメタン富化ガス流を生成させる工程;及び
(f)第2のガス流(又は存在する場合第2のメタン富化ガス流)を回収する工程;
を含み、
ここで、
(i)工程(c)及び工程(e)の少なくとも一つが存在し、
(ii)第2のガス流(又は存在する場合第2のメタン富化ガス流)がメタン生成物流であるか、又は第2のガス流(又は存在する場合第2のメタン富化ガス流)を精製して、メタン生成物流を発生させ、
(iii)固形チャー生成物が、工程(b)で生成され、これは触媒ガス化装置から定期
的に取出され、
(iv)第1のガス流中の一酸化炭素の一部を二酸化炭素に変換し、第1のガス流中の水素の割合を増やすために水性媒体の存在のもと、第1のガス流に水−ガス・シフト反応を施す、
上記方法。 - 工程(a)、(b)、(d)及び(f)、及び存在する場合、(c)及び(e)が連続である、請求項1の方法。
- 炭素質フィードストックが、触媒ガス化装置中に導入される前に、ガス化触媒を添加され、及び炭素質フィードストックが、炭素原子に対するアルカリ金属原子の比を0.01〜0.10の範囲にするのに十分な量のアルカリ金属ガス化触媒を添加されることを特徴とする、請求項1又は2に記載の方法。
- メタン生成物流が、パイプライン品質の天然ガスに相当することを特徴とする、請求項1〜3のいずれかに記載の方法。
- 工程(e)が存在することを特徴とする、請求項1〜4のいずれかに記載の方法。
- 第1のガス流が、触媒ガス化装置に供給される過熱スチームを生成するために取出される熱エネルギーを含むことを特徴とする、請求項1〜5のいずれかに記載の方法。
- 炭素燃料燃焼の過熱器が存在しないことを特徴とする、請求項1〜6のいずれかに記載の方法。
- 第1のガス流が、第1のガス流中のメタン、二酸化炭素、一酸化炭素、及び水素のモルに基づいて、少なくとも20mol%のメタンを含むことを特徴とする、請求項1〜7のいずれかに記載の方法。
- 触媒ガス化装置に供給される酸素の総量が、触媒ガス化装置に供給されるスチームの容積に基づいて、3容積%より大きく15容積%の範囲であることを特徴とする、請求項1〜8のいずれかに記載の方法。
- 触媒ガス化装置に供給される、酸素の総量が、炭素質フィードストックの質量部あたり、0.05〜1.0質量部のO2の範囲であることを特徴とする、請求項1〜9のいずれかに記載の方法。
- 固形チャー生成物が、取出され、触媒回収ユニットに送られることを特徴とする、請求項1〜10のいずれかに記載の方法。
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AU2009293087A1 (en) | 2010-03-25 |
US20100076235A1 (en) | 2010-03-25 |
CN102159682A (zh) | 2011-08-17 |
KR20110073523A (ko) | 2011-06-29 |
AU2009293087B2 (en) | 2012-11-15 |
CA2735137C (en) | 2013-05-21 |
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