JP2011148969A - 水素化分解法用添加物、その製造法及び使用法 - Google Patents
水素化分解法用添加物、その製造法及び使用法 Download PDFInfo
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Abstract
【解決手段】水素化分解法の添加物は、粒径約0.1〜約2,000μm、嵩密度約500〜約2,000kg/m3、見かけ密度約1,000〜約2,000kg/m3及び湿気0〜約5重量%を有する固体有機材料を含む。水素化分解工程用添加物の製造法及び使用法も提供する。本発明の添加物を使用して、高い転換レベルで水素化分解法を実施できる。
【選択図】図1
Description
例1は、アスファルテン、コークス及び/又は重縮合環式芳香族化合物の炭素質添加物による捕捉性能を示す。
例2は、炭素質添加物の金属捕捉率を示す。
図1に示す装置により、下記実験を行った。
図1に示す装置により、下記実験を行った。
holdup)が2倍に増大するので、反応量が改善され、高転化率が得られる。
Claims (30)
- 粒径約0.1〜約2,000μm、嵩密度約500〜約2,000kg/m3、見かけ密度約1,000〜約2,000kg/m3、及び湿気0〜約5重量%を有する固体有機物質を含むことを特徴とする水素化分解工程用添加物。
- 粒径は、約20〜約1,000μmである請求項1に記載の水素化分解工程用添加物。
- 第1の精粒領域に未処理炭素質材料を供給して、未処理炭素質材料の粒径より小さい粒径の精粒材料を生成する工程と、
精粒材料を乾燥させて、約5重量%未満の湿気を有する乾燥精粒材料を生成する工程と、
分類領域に乾燥精粒材料を供給して、所望の粒度基準に適合しない乾燥精粒材料の粒子と所望の粒度基準に適合する粒子とを分離する工程と、
所望の粒度基準に適合する粒子を温度約300〜約1,000℃に加熱する工程と、
加熱された粒子を加熱工程から取り出して、約80℃未満の温度に冷却して、添加物を生成する工程とを含むことを特徴とする水素化分解工程用添加物の製造法。 - 所望の粒度基準に適合しない粒子を精粒工程に再び搬送して、再精粒材料を生成する工程と、
再精粒材料を再び分類領域に搬送して、所望の粒度基準に適合しない再精粒粒子と所望の粒度基準に適合する再精粒粒子とを分離する工程と、
分類領域でも未だ所望の粒度基準に適合しない再精粒粒子を再生する工程とを更に含む請求項3に記載の水素化分解工程用添加物の製造法。 - 加熱工程前に、所望の粒度基準に適合する初期の粒子に、所望の粒度基準に適合する再精粒粒子を加える工程を含む請求項4に記載の水素化分解工程用添加物の製造法。
- 所望の温度を有する空気流中に粒子を曝して、粒子を加熱しかつ冷却する工程とを含む請求項3に記載の水素化分解工程用添加物の製造法。
- 加熱工程前に、所望の粒度基準に適合する粒子を第2の分類領域に搬送する工程と、
第2の分類領域で所望の粒度基準に適合するものと再度分類した粒子を加熱工程に搬送する工程と、
第2の分類領域で所望の粒度基準に適合しないものと再度分類した粒子を集塊所に搬送する工程とを含む請求項3に記載の水素化分解工程用添加物の製造法。 - 冷却工程後の添加物を最終分類領域に搬送する工程と、
最終分類領域で所望の粒度基準に適合しない添加物粒子と所望の粒度基準に適合する添加物粒子とを分離する工程と、
所望の粒度基準に適合しない添加物粒子を集塊所に搬送する工程とを更に含む請求項3に記載の水素化分解工程用添加物の製造法。 - 粒径約0.1〜約2,000μm、嵩密度約500〜約2,000kg/m3、見かけ密度約1,000〜約2,000kg/m3及び湿気0〜約5重量%を有する固体有機材料を含む添加物を生成する工程を含む請求項3に記載の水素化分解工程用添加物の製造法。
- 粒径は、約20〜約1,000μmである請求項9に記載の水素化分解工程用添加物の製造法。
- バナジウム及びニッケルから成る群から選択される少なくとも1種の原料金属を含む重質原料、8族〜10族の少なくとも1種の金属及び6族の少なくとも1種の金属を含む触媒エマルジョン、水素並びに有機添加物を水素化分解状態の下で水素化分解領域に供給する工程と、
8族〜10族の前記金属、6族の前記金属及び少なくとも1種の原料金属を含む固体炭素系物質と、改質された炭化水素生成物とを生成する工程とを含み、
有機添加物は、粒径約0.1〜約2,000μm、嵩密度約500〜約2,000kg/m3、見かけ密度約1,000〜約2,000kg/m3及び湿気0〜約5重量%を有する固体有機物質を含むことを特徴とする水素化分解法。 - 原料に対して約0.5〜約5重量%の量で有機添加物を供給する工程を含む請求項11に記載の水素化分解法。
- 約4cm/s以上の気体速度で水素化分解反応させる工程を含む請求項11に記載の水素化分解法。
- 少なくともアスファルテン転化率約75重量%と、少なくともコンラドソン炭素転化率約70重量%を有する水素化分解を発生する工程を含む請求項11に記載の水素化分解法。
- 減圧残油、重質原油、超重質原油及びそれらの組み合せから成る群から重質原料を選択する工程を含む請求項11に記載の水素化分解法。
- 重質原料は、減圧残油である請求項11に記載の水素化分解法。
- 重質原料の比重は、約1.07〜約1.02(API度1〜7)である請求項11に記載の水素化分解法。
- 重質原料の金属組成は、約200〜約2,000重量ppmである請求項11に記載の水素化分解法。
- 重質原料の金属組成は、バナジウム及びニッケルを含有する請求項11に記載の水素化分解法。
- 触媒エマルジョンは、8族〜10族の金属を含む第1の触媒エマルジョンと、6族の金属を含む第2の触媒エマルジョンとを含む請求項11に記載の水素化分解法。
- ニッケル、コバルト、鉄及びそれらの組み合せから成る群から8族〜10族の金属を選択する工程を含む請求項11に記載の水素化分解法。
- モリブデン、タングステン及びそれらの組み合せから成る群から6族の金属を選択する工程を含む請求項11に記載の水素化分解法。
- 6族の金属は、6族の硫化金属塩の形態である請求項11に記載の水素化分解法。
- 有機添加物は、コークス粒子を含む請求項11に記載の水素化分解法。
- 前記工程を連続して実施する工程を含む請求項11に記載の水素化分解法。
- 循環しない貫流方式で原料を使用して前記工程を実施する工程を含む請求項25に記載の水素化分解法。
- 水素化分解状態の反応器圧力は、約13〜約21MPaG(約130〜約210barg)、反応器温度は、約430〜約470℃である請求項11に記載の水素化分解法。
- 約50〜約1,000重量ppmの触媒金属と重質原料との重量比率となる量で、触媒エマルジョンと重質原料とを反応器に供給する工程を含む請求項11に記載の水素化分解法。
- 固体炭素系物質を除く重量基準による生産収量は、重質原料の重量を超える請求項11に記載の水素化分解法。
- 水素化分解領域は、上向並流三相気泡塔型反応器を備える請求項11に記載の水素化分解法。
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US20130048540A1 (en) | 2011-08-29 | 2013-02-28 | Intevep, S.A. | Ultra-dispersed catalyst and method for preparing same |
FR2998812B1 (fr) | 2012-12-05 | 2014-11-21 | IFP Energies Nouvelles | Injection d'additif dans une unite de synthese d'hydrocarbures a partir de gaz de synthese permettant de controler et maintenir une concentration homogene en catalyseur |
CA2941568A1 (en) | 2015-08-31 | 2017-02-28 | University Of New Brunswick | Process for upgrading heavy hydrocarbon liquids |
AU2017289220B2 (en) * | 2016-06-28 | 2022-03-24 | Carbonx Ip 3 B.V. | Production of crystalline carbon structure networks |
CA2982067A1 (en) | 2016-10-07 | 2018-04-07 | Ying Zheng | Catalytic process for co-processing of lignocellulosic biomass and heavy petroleum fuels |
CN108165295B (zh) * | 2018-01-10 | 2020-08-14 | 广昌达新材料技术服务(深圳)股份有限公司 | 一种用于炼油过程延迟焦化的液体增收剂 |
US11473024B2 (en) * | 2018-04-18 | 2022-10-18 | Exxonmobil Chemical Patents Inc. | Processing pyrolysis tar particulates |
CN109092505A (zh) * | 2018-07-10 | 2018-12-28 | 丰城黑豹炭黑有限公司 | 一种用于加工炭黑的一体化设备 |
EP3918037A1 (en) | 2019-01-29 | 2021-12-08 | SABIC Global Technologies B.V. | Conversion of heavy ends of crude oil or whole crude oil to high value chemicals using a combination of thermal hydroprocessing, hydrotreating with steam crackers under high severity conditions to maximize ethylene, propylene, butenes and benzene |
WO2020157595A1 (en) | 2019-01-29 | 2020-08-06 | Sabic Global Technologies B.V. | Methods and systems for upgrading crude oils, heavy oils, and residues |
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US8835351B2 (en) | 2014-09-16 |
CU20100135A7 (es) | 2012-06-21 |
ECSP10010221A (es) | 2011-08-31 |
CA2704879A1 (en) | 2011-07-21 |
EP2348092A1 (en) | 2011-07-27 |
RU2010123026A (ru) | 2011-12-20 |
US20130143735A1 (en) | 2013-06-06 |
US20130130033A1 (en) | 2013-05-23 |
JP2014055301A (ja) | 2014-03-27 |
CN102134506A (zh) | 2011-07-27 |
MX2010006032A (es) | 2011-07-21 |
JP5630928B2 (ja) | 2014-11-26 |
KR20110085838A (ko) | 2011-07-27 |
RU2541324C2 (ru) | 2015-02-10 |
US9168506B2 (en) | 2015-10-27 |
CU23865B1 (es) | 2013-03-27 |
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CN103820144A (zh) | 2014-05-28 |
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