WO2016201955A1 - 芳香烃、对二甲苯和对苯二甲酸的制造方法 - Google Patents
芳香烃、对二甲苯和对苯二甲酸的制造方法 Download PDFInfo
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- WO2016201955A1 WO2016201955A1 PCT/CN2016/000315 CN2016000315W WO2016201955A1 WO 2016201955 A1 WO2016201955 A1 WO 2016201955A1 CN 2016000315 W CN2016000315 W CN 2016000315W WO 2016201955 A1 WO2016201955 A1 WO 2016201955A1
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- aromatic hydrocarbon
- oxide
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- B01J29/405—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
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- B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
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- B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
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Definitions
- the present invention relates to a process for producing an aromatic hydrocarbon, and more particularly to a process for producing a BTX aromatic hydrocarbon in a high carbon yield.
- the invention further relates to a process for the manufacture of para-xylene and terephthalic acid based on the process for the production of said aromatic hydrocarbons.
- auxiliary agent 0 to 10 parts by weight (preferably 0.01 to 10 parts by weight, more preferably 0.01 to 6 parts by weight) of the auxiliary agent
- the auxiliary agent is selected from the group consisting of Na, Ca, K, Be, Mg, Ba, V, Nb, Cr , one or more of Mo, W, Mn, Re, Fe, Co, Ni, Cu, Zn, Ga, Ru, Pd, Pt, Ag, B, Al, Sn, P, Sb, La, and Ce
- SiO 2 /Al 2 O 3 6 to 35
- the metal oxide has a sulfated ratio of 0.5 to 25 wt%, preferably 1 to 8 wt%,
- hydrocarbons or hydrocarbon derivative groups of more than 3 carbon atoms such as propyl, propoxy, butyl, unless otherwise explicitly defined, or the meaning is beyond the understanding of those skilled in the art
- butane, butene, butenyl, hexane, etc. have the same meaning as when the prefix is "positive" when the prefix is "positive”.
- propyl is generally understood to be n-propyl
- butyl is generally understood to be n-butyl.
- biomass material examples include paper sludge, waste paper, bagasse, glucose, wood, corn cob, corn stover, and straw straw. These biomass materials may be used singly or in combination of two or more.
- the biomass content in the biomass material is usually from 30 to 99% by weight
- the hemicellulose content is usually from 0 to 50%
- the lignin content is usually from 0 or 1 to 40%.
- these molecular sieve compositions can be produced directly using commercially available products or by methods known in the art.
- a method of producing the molecular sieve composition for example, a method of mixing a molecular sieve, a binder, and a co-extruding agent, a pore-expanding agent, and water, which are used as needed, into a mixture, extruding a strip, and then It is dried at 100-200 ° C for 1-24 hours and then calcined at 400-700 ° C for 1-10 hours.
- the contacting step can be carried out in one or more reactors.
- a bed reactor in particular, a fixed bed reactor, a fluidized bed reactor, an ebullated bed reactor or a combination thereof may be mentioned.
- the operation mode of the reactor may be either a batch mode or a continuous mode, and is not particularly limited.
- test results are described in the context of the present specification using aromatic hydrocarbon carbon yields and BTX aromatic hydrocarbon carbon yields, wherein the BTX aromatic hydrocarbon carbon yield is the primary comparative indicator.
- the aromatic hydrocarbon carbon yield and the BTX aromatic hydrocarbon carbon yield were calculated according to the following formula.
- the reaction pressure is 1.2 MPa
- the reaction temperature is 130 ° C
- the hydrogen/levulinic acid molar ratio is 10
- the levulinic acid space velocity is 0.3 h -1
- the levulinic acid conversion rate is 89%
- ⁇ -penta The molar selectivity of the lactone was 4.5%
- the molar selectivity of methyltetrahydrofuran was 94.3%. 248 kg of levulinic acid was hydrogenated to form 8.5 kg of ⁇ -valerolactone to give 154.1 kg of methyltetrahydrofuran.
- the raw material was 1 ton of cellulose and the dry cellulose content was 98.3%.
- the cellulose was stirred and mixed with 3.5 tons of a 3.7% aqueous solution of sulfuric acid, and the acid solution was completed by maintaining the mixed solution at 3.0 MPa and 205 ° C for 30 minutes under stirring, and the liquid phase product was separated to obtain 511 kg of acetyl.
- 194 kg of formic acid was decomposed to give 8.3 kg of hydrogen.
- the reaction pressure was 4.0 MPa
- the reaction temperature was 196 ° C
- the hydrogen/furfural molar ratio was 60
- the furfural space velocity was 0.5 h -1
- the furfural conversion rate was 99%.
- the selectivity of 2-methyltetrahydrofuran is 99%.
- 83.1 kg of furfural was subjected to hydrogenation reaction to give 36.7 kg of methyltetrahydrofuran.
- the hydrogen used for the hydrogenation of levulinic acid and furfural is partially decomposed from formic acid.
- the catalyst activity was evaluated on a fixed bed.
- the reaction mass of the catalyst was 3 g
- the reaction substrate was methyl levulinate
- the weight space velocity was 3.0 hr -1
- the hydrogen pressure was 2.0 MPa
- the flow rate was 50 ml min -1
- the temperature was 450 °C.
- the conversion of the reaction substrate was 93%
- the selectivity of the BTX aromatic hydrocarbon was 78%
- the carbon yield of the BTX aromatic hydrocarbon was 73%.
- the catalyst activity was evaluated on a fixed bed.
- the reaction mass of the catalyst was 3 g
- the reaction substrate was butyl levulinate
- the weight space velocity was 1.0 hour -1
- the hydrogen pressure was 1.0 MPa
- the flow rate was 50 ml min -1
- the temperature was 400 °C.
- the conversion of the reaction substrate was 88%
- the selectivity of the BTX aromatic hydrocarbon was 77%
- the carbon yield of the BTX aromatic hydrocarbon was 68%.
- the catalyst activity was evaluated on a fixed bed.
- the reaction mass of the catalyst was 3 g
- the reaction substrate was ethyl levulinate
- the weight space velocity was 3.0 hr -1
- the hydrogen pressure was 1.0 MPa
- the flow rate was 50 ml min -1
- the temperature was 550 °C.
- the conversion of the reaction substrate was 99%
- the selectivity of the BTX aromatic hydrocarbon was 83%
- the carbon yield of the BTX aromatic hydrocarbon was 82%.
- the catalyst activity was evaluated on a fixed bed.
- the reaction mass of the catalyst was 3 g
- the reaction substrate was butyl levulinate
- the weight space velocity was 1.0 hour -1
- the hydrogen pressure was 1.0 MPa
- the flow rate was 50 ml min -1
- the temperature was 400 °C.
- the conversion of the reaction substrate was 94%
- the selectivity of the BTX aromatic hydrocarbon was 88%
- the carbon yield of the BTX aromatic hydrocarbon was 83%.
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Abstract
Description
实施例 | 底物 | 催化剂 | 硅铝比 | 转化率/% | BTX选择性/% |
1 | 乙酰丙酸 | ZSM-5 | 25 | 96 | 82 |
2 | 乙酰丙酸 | ZSM-5 | 150 | 94 | 93 |
3 | 乙酰丙酸 | ZSM-5 | 500 | 91 | 86 |
4 | 乙酰丙酸 | beta | 30 | 89 | 78 |
5 | 乙酰丙酸 | beta | 100 | 85 | 71 |
6 | 乙酰丙酸 | MCM-41 | 50 | 89 | 76 |
7 | 乙酰丙酸 | MCM-22 | 70 | 91 | 83 |
8 | 乙酰丙酸 | MCM-41 | 150 | 86 | 76 |
实施例 | 底物 | 催化剂 | 转化率/% | BTX选择性/% |
1 | 乙酰丙酸 | SO4 2-/ZrO2 | 83 | 87 |
2 | 乙酰丙酸 | S2O8 2-/ZrO2 | 98 | 93 |
3 | 乙酰丙酸 | SO4 2-/TiO2 | 88 | 81 |
4 | 乙酰丙酸 | SO4 2-/ZrO2-Fe3O4 | 82 | 78 |
5 | 乙酰丙酸 | Pt/SO4 2-/TiO2 | 89 | 81 |
6 | 乙酰丙酸 | SO4 2-/TiO2-ZrO2 | 87 | 81 |
7 | 乙酰丙酸 | SO4 2-/ZrO2-WO3 | 92 | 90 |
8 | 乙酰丙酸 | SO4 2-/ZrO2-Fe2O3-Cr2O3 | 94 | 87 |
实施例 | 底物 | 催化剂 | 转化率/% | BTX选择性/% |
1 | 乙酰丙酸 | SO4 2-/ZrO2 | 99 | 93 |
2 | 乙酰乙酸 | S2O8 2-/ZrO2 | 90 | 93 |
3 | 乙酰丙酸 | SO4 2-/TiO2 | 89 | 87 |
4 | 乙酰乙酸乙酯 | SO4 2-/ZrO2-Fe3O4 | 86 | 83 |
5 | 乙酰丙酸甲酯 | Pt/SO4 2-/TiO2 | 85 | 82 |
6 | 乙酰丁酸甲酯 | SO4 2-/TiO2-ZrO2 | 89 | 87 |
7 | 乙酰丙酸辛酯 | SO4 2-/TiO2-Al2O3 | 87 | 85 |
8 | 乙酰丙酸乙酯 | SO4 2-/ZrO2-Fe2O3-Cr2O3 | 91 | 85 |
9 | 乙酰丙酸丁酯 | SbF5/SiO2-Al2O3 | 98 | 89 |
10 | 乙酰丙酸乙酯 | SO4 2-/TiO2-WO3 | 89 | 86 |
11 | 乙酰丙酸癸酯 | SO4 2-/ZrO2-WO3 | 91 | 84 |
12 | 乙酰丙酸甲酯 | SO4 2-/TiO2-MoO3 | 86 | 83 |
13 | 乙酰丙酸甲酯 | BiF3/Al2O3-B2O3 | 96 | 86 |
14 | 乙酰己酸甲酯 | NbF3/Al2O3-B2O3 | 88 | 94 |
15 | 乙酰丙酸丁酯 | SO4 2-/ZrO2-Fe2O3-MnO2 | 89 | 87 |
16 | 乙酰丙酸丁酯 | SO4 2-/ZrO2-Fe2O3-Cr2O3 | 92 | 86 |
17 | 乙酰丙酸丁酯 | AlCl3-CuCl2 | 87 | 82 |
实施例 | 底物 | 催化剂 | 转化率/% | BTX选择性/% |
1 | 乙酰丙酸 | WO3/ZrO2 | 97 | 93 |
2 | 乙酰乙酸 | WO3/ZrO2 | 91 | 92 |
3 | 乙酰丙酸 | WO3/ZrO2 | 86 | 86 |
4 | 乙酰乙酸乙酯 | MoO3/ZrO2 | 99 | 89 |
5 | 乙酰丙酸甲酯 | CeO2/ZrO2 | 82 | 94 |
6 | 乙酰丁酸甲酯 | WO3/ZrO2 | 93 | 83 |
7 | 乙酰丙酸辛酯 | MoO3/ZrO2 | 95 | 85 |
8 | 乙酰丙酸乙酯 | La2O3/ZrO2 | 93 | 85 |
9 | 乙酰丙酸丁酯 | WO3/ZrO2 | 93 | 87 |
10 | 乙酰丙酸乙酯 | WO3/ZrO2 | 99 | 83 |
11 | 乙酰丙酸癸酯 | MoO3/ZrO2 | 96 | 84 |
12 | 乙酰丙酸甲酯 | MnO2/ZrO2 | 87 | 83 |
Claims (15)
- 根据权利要求1所述的制造方法,其中所述芳构化反应条件包括:反应温度300至800℃,优选300至650℃,反应压力0.1至10.0MPa,优选0.5至6.0MPa,氢气压力以表压计0.1至5MPa,优选0.5至4MPa,含氧原料重量空速0.3至10小时-1,优选0.3至5小时-1。
- 根据权利要求1所述的制造方法,其中所述含氧原料衍生自生物质材料,优选衍生自木糖醇、葡萄糖、纤维二糖、纤维素、半纤维素和木质素中的一种或多种、或者衍生自造纸污泥、废纸、甘蔗渣、葡萄糖、木材、玉米芯、玉米秸和稻草秸秆中的一种或多种。
- 根据权利要求1所述的制造方法,其中所述芳构化催化剂选自固体酸催化剂中的一种或多种,优选选自分子筛、固体超强酸和复合金属氧化物中的一种或多种。
- 根据权利要求1所述的制造方法,其中所述分子筛选自ZSM型分子筛(优选选自ZSM-5、ZSM-11、ZSM-22、ZSM-23和ZSM-38中的一种或多种)、Y型分子筛、beta型分子筛、L型分子筛、MCM型分子筛(优选选自MCM-22和MCM-41中的一种或多种)中的一种或多种,优选选自ZSM-5、Y型分子筛、beta型分子筛和MCM-41中的一种或多种,更特别是ZSM-5或M/ZSM-5(其中M选自Zn、Ga、Sn或其组合)。
- 根据权利要求5所述的制造方法,其中所述分子筛是分子筛组合 物,其包含以下组份:a)20至80重量份(优选30至70重量份)所述分子筛,b)20至80重量份(优选30至70重量份)粘结剂(优选选自硅溶胶、拟薄水铝石、氧化铝、经酸处理后粘土、高岭土、蒙脱土、膨润土中的一种或多种,更优选选自拟薄水铝石、氧化铝和硅溶胶中的一种或多种,c)0至10重量份(优选0.01至10重量份,更优选0.01至6重量份)助剂,其中所述助剂选自Na、Ca、K、Be、Mg、Ba、V、Nb、Cr、Mo、W、Mn、Re、Fe、Co、Ni、Cu、Zn、Ga、Ru、Pd、Pt、Ag、B、Al、Sn、P、Sb、La和Ce中的一种或多种,优选选自Ca、K、Mg、Cr、Mo、Fe、Ni、Cu、Zn、Ga、Ru、Pd、Pt、Ag、B、Sn、P、La和Ce中的一种或多种,更优选选自Zn、Ga和Sn中的一种或多种。
- 根据权利要求5所述的制造方法,其中所述ZSM型分子筛的硅铝摩尔比SiO2/Al2O3=10至500,优选SiO2/Al2O3=15至100或15至200,所述Y分子筛的硅铝摩尔比SiO2/Al2O3=2至70,优选SiO2/Al2O3=3至50或5至50,所述beta分子筛的硅铝摩尔比SiO2/Al2O3=10至150,优选SiO2/Al2O3=15至65或50至100,所述L型分子筛的硅铝摩尔比SiO2/Al2O3=5至100,优选SiO2/Al2O3=6至35,所述MCM型分子筛的硅铝摩尔比SiO2/Al2O3=20至250,优选SiO2/Al2O3=32至150。
- 根据权利要求4所述的制造方法,其中所述固体超强酸选自路易斯酸负载型固体超强酸、无机金属盐/路易斯酸复合型固体超强酸和硫酸化金属氧化物型固体超强酸中的一种或多种。
- 根据权利要求8所述的制造方法,其中所述路易斯酸负载型固体超强酸的载体选自元素周期表第IIIA族元素的固体氧化物和第IVA族元素的固体氧化物中的一种或多种,优选选自SiO2、B2O3和Al2O3中的一种或多种,所述路易斯酸负载型固体超强酸的路易斯酸选自元素周期表第VB族元素的卤化物(优选氟化物)、第IIIA族元素的卤化物(优选氟化物)和第VA族元素的卤化物(优选氟化物)中的一种或多种,优选选自元素周期表第VB族元素的卤化物(优选氟化物)和第VA族元素的卤化物(优选氟化物)中的一种或多种,进一步优选选自PF3、AsF3、SbF3、BiF3、SbF5、TaF3、VF3和NbF3中的一种或多种,所述路易斯酸负载型固体超强酸优选选自SbF5/SiO2-Al2O3、PF3/Al2O3-B2O3、AsF3/Al2O3-B2O3、SbF3/Al2O3-B2O3、BiF3/Al2O3-B2O3、TaF3/Al2O3-B2O3、VF3/Al2O3-B2O3和NbF3/Al2O3-B2O3中的一种或多种,所述无机金属盐/路易斯酸复合型固体超强酸的无机金属盐选自元素周期表第IB族金属元素的无机酸盐(优选氢卤酸盐,更优选盐酸盐)、第IIB族金属元素的无机酸盐(优选氢卤酸盐,更优选盐酸盐)、第VII族金属元素的无机酸盐(优选氢卤酸盐,更优选盐酸盐)和第VIII族金属元素的无机酸盐(优选氢卤酸盐,更优选盐酸盐)中的一种或多种,优选CuCl2,所述无机金属盐/路易斯酸复合型固体超强酸的路易斯酸选自元素周期表第VB族元素的卤化物(优选氯化物)、第IIIA族元素的卤化物(优选氯化物)和第VA族元素的卤化物(优选氯化物)中的一种或多种,优选选自元素周期表第IIIA族元素的卤化物(优选氯化物)中的一种或多种,优选AlCl3,所述无机金属盐/路易斯酸复合型固体超强酸优选AlCl3-CuCl2,所述硫酸化金属氧化物型固体超强酸的金属氧化物是元素周期表第IVB族金属元素的氧化物A(优选选自ZrO2和TiO2中的一种或多种)或者是所述氧化物A被选自元素周期表第IIIA族金属元素(以氧化物形式存在)、第VIIB族金属元素(以氧化物形式存在)、第VIII族贵金属元素(以金属单质形式存在)、第VIII族贱金属元素(以氧化物形式存在)、第VIB族金属元素(以氧化物形式存在)和镧系金属元素(以氧化物形式存在)中的一种或多种改性元素(优选选自Fe、Pt、Re、Al、W、Cr、Mo和Mn中的一种或多种)改性而获得的氧化物B,所述硫酸化金属氧化物型固体超强酸优选选自SO4 2-/ZrO2、S2O8 2-/ZrO2、SO4 2-/TiO2、SO4 2-/ZrO2-Fe3O4、Pt/SO4 2-/TiO2、SO4 2-/TiO2-ZrO2、SO4 2-/TiO2-Al2O3、SO4 2-/TiO2-WO3、SO4 2-/ZrO2-Fe2O3-Cr2O3、SO4 2-/ZrO2-WO3、SO4 2-/TiO2-MoO3和SO4 2-/ZrO2-Fe2O3-MnO2中的一种或多种。
- 根据权利要求9所述的制造方法,其中在所述路易斯酸负载型固体超强酸中,相对于所述载体的重量,所述路易斯酸的负载量为1至30wt%,优选1至15wt%,所述无机金属盐/路易斯酸复合型固体超强酸中,所述无机金属盐与 所述路易斯酸的重量比例为1至30∶100,优选1至15∶100,所述硫酸化金属氧化物型固体超强酸中,所述金属氧化物的硫酸化率为0.5至25wt%,优选1至8wt%,所述氧化物B中,以氧化物形式存在的所述改性元素(以氧化物计)与所述氧化物A的重量比例为0.1至25∶100,优选0.5至10∶100,以金属单质形式存在的所述改性元素(以金属计)与所述氧化物A的重量比例为0.1至15∶100,优选0.3至6∶100。
- 根据权利要求4所述的制造方法,其中所述复合金属氧化物是元素周期表第IVB族金属元素的氧化物C(优选选自ZrO2和TiO2中的一种或多种,更优选ZrO2)与选自元素周期表第IIIA族金属元素的氧化物、第VII族金属元素的氧化物、第VIB族金属元素的氧化物和镧系金属元素的氧化物中的一种或多种氧化物D(优选选自B2O3、Al2O3、MnO2、Cr2O3、CrO3、MoO3、WO3、La2O3和CeO2中的一种或多种,更优选选自MnO2、MoO3、WO3、La2O3和CeO2中的一种或多种)的复合氧化物,优选ZrO2与选自MnO2、Mo2O3、WO3、La2O3和CeO2中的一种或多种氧化物D的复合氧化物。
- 根据权利要求11所述的制造方法,其中所述氧化物C与所述氧化物D比例,以重量份数计,为60至99.9∶0.1至40,优选60至99∶1至40。
- 根据权利要求1所述的制造方法,还包括使生物质材料进行催化转化,获得所述含氧原料的步骤。
- 一种对二甲苯的制造方法,包括以下步骤:按照权利要求1-13任一项所述的方法制造芳香烃的步骤;和从所述芳香烃中分离出对二甲苯的步骤。
- 一种对苯二甲酸的制造方法,包括以下步骤:按照权利要求14所述的方法制造对二甲苯的步骤;和将对二甲苯转化为对苯二甲酸的步骤。
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KR102454225B1 (ko) | 2022-10-12 |
EP3312153B1 (en) | 2021-05-05 |
EP3312153A4 (en) | 2019-02-13 |
KR20180019699A (ko) | 2018-02-26 |
BR112017027347B1 (pt) | 2022-06-21 |
JP2018524319A (ja) | 2018-08-30 |
BR112017027347A2 (pt) | 2019-02-19 |
EP3312153A1 (en) | 2018-04-25 |
ES2880326T3 (es) | 2021-11-24 |
DK3312153T3 (da) | 2021-07-26 |
JP6877367B2 (ja) | 2021-05-26 |
US10358606B2 (en) | 2019-07-23 |
US20180282631A1 (en) | 2018-10-04 |
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