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RU2012157780A - Способ получения метана из биомассы - Google Patents

Способ получения метана из биомассы Download PDF

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Publication number
RU2012157780A
RU2012157780A RU2012157780/04A RU2012157780A RU2012157780A RU 2012157780 A RU2012157780 A RU 2012157780A RU 2012157780/04 A RU2012157780/04 A RU 2012157780/04A RU 2012157780 A RU2012157780 A RU 2012157780A RU 2012157780 A RU2012157780 A RU 2012157780A
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RU
Russia
Prior art keywords
methane
product
stream
hydroconversion
coal
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RU2012157780/04A
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English (en)
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RU2573567C2 (ru
Inventor
Терри Л. МАРКЕР
Ларри Дж. ФЕЛИКС
Мартин Б. ЛИНК
Ховард С. Мейер
Деннис Леппин
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Гэз Текнолоджи Инститьют
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Publication of RU2012157780A publication Critical patent/RU2012157780A/ru
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Publication of RU2573567C2 publication Critical patent/RU2573567C2/ru

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Abstract

1. Способ получения метана из биомассы, включающий следующие стадии:а) гидропиролиз биомассы в реакторном сосуде гидропиролиза, содержащем молекулярный водород и катализатор дезоксигенирования, при температуре гидропиролиза выше приблизительно 1000°F (538°C) и при давлении гидропиролиза в интервале от приблизительно 100 до приблизительно 600 фунт/кв.дюйм (690-4140 кПа) с получением одиночного выпускного потока продукта гидропиролиза, содержащего уголь и газ;b) отделение указанного угля от указанного продукта гидропиролиза с получением продукта гидропиролиза со сниженным содержанием угля;с) гидроконверсия указанного продукта гидропиролиза со сниженным содержанием угля в реакторном сосуде гидроконверсии с использованием катализатора гидроконверсии при температуре гидроконверсии выше приблизительно 800°F (427°C) и при давлении гидроконверсии в интервале от приблизительно 100 до приблизительно 600 фунт/кв.дюйм (690-4140 кПа) с получением продукта гидроконверсии;d) охлаждение и введение указанного продукта гидроконверсии в реактор конверсии вода-газ, получение продукта конверсии вода-газ, содержащего воду и газообразную смесь, содержащую СО, Ни метан; ие) разделение указанных СО, Ни метана с получением потока СО, потока Ни потока метанового продукта.2. Способ по п. 1, в котором, по меньшей мере, часть указанного потока метанового продукта вводят в установку парового реформинга, в которой указанный метан подвергается реформингу с получением СО-реформера и Н-реформера.3. Способ по п. 2, в котором, по меньшей мере, часть указанного Н-реформера вводится в реактор метанирования вместе с потоком метанового продукта, взаимодействует с лю

Claims (20)

1. Способ получения метана из биомассы, включающий следующие стадии:
а) гидропиролиз биомассы в реакторном сосуде гидропиролиза, содержащем молекулярный водород и катализатор дезоксигенирования, при температуре гидропиролиза выше приблизительно 1000°F (538°C) и при давлении гидропиролиза в интервале от приблизительно 100 до приблизительно 600 фунт/кв.дюйм (690-4140 кПа) с получением одиночного выпускного потока продукта гидропиролиза, содержащего уголь и газ;
b) отделение указанного угля от указанного продукта гидропиролиза с получением продукта гидропиролиза со сниженным содержанием угля;
с) гидроконверсия указанного продукта гидропиролиза со сниженным содержанием угля в реакторном сосуде гидроконверсии с использованием катализатора гидроконверсии при температуре гидроконверсии выше приблизительно 800°F (427°C) и при давлении гидроконверсии в интервале от приблизительно 100 до приблизительно 600 фунт/кв.дюйм (690-4140 кПа) с получением продукта гидроконверсии;
d) охлаждение и введение указанного продукта гидроконверсии в реактор конверсии вода-газ, получение продукта конверсии вода-газ, содержащего воду и газообразную смесь, содержащую СО2, Н2 и метан; и
е) разделение указанных СО2, Н2 и метана с получением потока СО2, потока Н2 и потока метанового продукта.
2. Способ по п. 1, в котором, по меньшей мере, часть указанного потока метанового продукта вводят в установку парового реформинга, в которой указанный метан подвергается реформингу с получением СО2-реформера и Н2-реформера.
3. Способ по п. 2, в котором, по меньшей мере, часть указанного Н2-реформера вводится в реактор метанирования вместе с потоком метанового продукта, взаимодействует с любым остаточным СО и/или СО2 в потоке метанового продукта и образует дополнительный метан.
4. Способ по п. 2, в котором указанная вода вводится в указанную установку парового реформинга для реформинга указанного метана.
5. Способ по п. 4, в котором дополнительная вода из внешнего по отношению к способу источника вводится в указанную установку парового реформинга для реформинга указанного метана.
6. Способ по п. 1, в котором первая часть указанного потока метанового продукта вводится в установку сжигания и сжигается, нагревая тем самым вторую часть указанного потока метанового продукта, и указанная вторая часть указанного потока метанового продукта вводится вместе с водяным паром в установку парового реформинга метана, образуя продукт-реформер СО, СО2 и Н2.
7. Способ по п. 1, в котором часть угля, отделенного от потока продуктов гидропиролиза, сжигается в печи, нагревая указанный поток метанового продукта, и указанный поток метанового продукта вводится в установку парового реформинга вместе с водой, образуя СО2-реформер и Н2-реформер.
8. Способ по п. 2, в котором часть указанного угля сжигается в камере сгорания парового котла с получением водяного пара, при этом этот пар вводится в установку парового реформинга вместе с частью указанного потока метана.
9. Способ по п. 6, в котором, по меньшей мере, часть указанного Н2-реформера вводится в реактор метанирования, где он взаимодействует с любым остаточным СО2 в потоке метанового продукта и образует дополнительный метан.
10. Способ по п. 2, в котором, по меньшей мере, часть указанного Н2-реформера рециклируют в указанный реакторный сосуд гидропиролиза для указанного гидропиролиза указанной биомассы.
11. Способ по п. 1, в котором указанный метан отделяется от указанной газовой смеси способом извлечения гидрата метана для того, чтобы снизить пропорцию потока метанового продукта, содержащего дополнительное количество Н2, который затем сразу рециклируют на стадию гидропиролиза.
12. Способ по п. 1, в котором, по меньшей мере, один из указанного катализатора дезоксигенирования и указанного катализатора гидроконверсии является стеклокерамическим материалом.
13. Способ по п. 1, в котором указанный гидропиролиз выполняется при массовой часовой пространственной скорости в интервале от приблизительно 0,2 до приблизительно 10 г биомассы/г катализатора/ч.
14. Способ по п. 1, в котором указанная гидроконверсия выполняется при массовой часовой пространственной скорости в интервале от приблизительно 0,2 до приблизительно 3 г биомассы/г катализатора/ч.
15. Способ по п. 1, в котором указанным реакторным сосудом гидропиролиза является реактор с псевдоожиженным слоем, содержащий псевдоожиженный слой.
16. Способ по п. 15, в котором время пребывания газа в указанном реакторном сосуде гидропиролиза составляет менее приблизительно одной минуты.
17. Способ по п. 15, в котором указанный уголь удаляется из указанного реактора с псевдоожиженным слоем по существу только из вышеуказанного псевдоожиженного слоя.
18. Способ по п. 1, в котором указанным реакторным сосудом гидропиролиза является реактор с псевдоожиженным слоем, содержащий псевдоожиженный слой, и указанный уголь удаляется из указанного реактора с псевдоожиженным слоем энергетическим отделением угля с использованием, по меньшей мере, одного из инерционного, электростатического и магнитного способов.
19. Способ по п. 1, в котором указанный катализатор дезоксигенирования выбран из группы, состоящей из сульфидированного СоМо, сульфидированного NiMo, каталитически активной стеклокерамики, боксита, угля и их смесей и комбинаций.
20. Способ по п. 1, в котором фильтр горячего газа, предварительно нагретый введением смесей или одиночных выбранных адсорбентов, используется для удаления выбранных загрязнений из газа, выходящего из одного из реакторного сосуда гидропиролиза и реакторного сосуда гидроконверсии.
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