CN102372550A - Method for preparing aromatic hydrocarbon through methanol transformation - Google Patents
Method for preparing aromatic hydrocarbon through methanol transformation Download PDFInfo
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- CN102372550A CN102372550A CN2010102617173A CN201010261717A CN102372550A CN 102372550 A CN102372550 A CN 102372550A CN 2010102617173 A CN2010102617173 A CN 2010102617173A CN 201010261717 A CN201010261717 A CN 201010261717A CN 102372550 A CN102372550 A CN 102372550A
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Abstract
The invention relates to a method for preparing aromatic hydrocarbon through methanol transformation, and mainly solves the problems of complicated process flow and low selectivity of target products existing in the prior art. The problems are better solved by adopting the technical scheme that the method comprises the step of: reacting by taking methanol as a raw material and a mixture of HZSM-5 containing rare earth metal or oxide thereof and at least one of a HZSM-11 or Hbeta molecular sieve as an active main body of a catalyst under the condition that the reaction temperature is 320 to 480 DEG C, the reaction pressure is 0.1 to 3.0MPa and the weight hourly space velocity of the raw material is 0.5 to 6.0 h<-1>; and the method can be used for the industrial production of the aromatic hydrocarbon through methanol transformation.
Description
Technical field
The present invention relates to a kind of method of methanol conversion for preparing arene.
Background technology
Since China's oil and natural gas source shortage, and coal resources are abundant relatively.In recent years, burning hot situation appears in China Coal Chemical Industry cause, the various places various Coal Chemical Industry projects that start one after another.As comparatively sophisticated coal chemical technology, coal-based synthesizing methanol becomes the first-selected project of most coal chemical industry enterprises.In recent years; China is that raw material production methyl alcohol is towards maximization, energy-saving development with coal; Output constantly increases, and therefore the production capacity of methyl alcohol will actively carry out the exploitation of Downstream Products of Methanol considerably beyond actual demand; Increase new methyl alcohol Application Areas, improve the production technology level of existing Downstream Products of Methanol, the development of methanol industry is had crucial meaning.
The methanol conversion research contents is very abundant.External Uop Inc., Lurgi company have developed MTO (methanol conversion system alkene respectively; Comprise ethene and propylene) and MTP (preparing propylene by methanol transformation) technology, Exxon-Mobil company has developed MTG (methanol conversion system gasoline) technology and MOGD (methanol conversion system petrol and diesel oil) technology.Domestic such as the Dalian Chemistry and Physics Institute and Shanxi coalification etc. also methanol conversion has been carried out a large amount of research, and aspect two of catalyzer and reaction process, obtained breakthrough.But no matter see from present circumstances, be to be high-quality gasoline with methanol conversion, still is converted into alkene, and the economy of process is all hindered owing to the restriction that receives added value of product makes its industrialization process.
Aromatic hydrocarbons (especially benzene (Benzene), toluene (Toluene) and YLENE (Xylene) are referred to as BTX) is important petrochemical complex basic raw material, has high added value.The aromatic hydrocarbons of China is mainly derived from petroleum resources, and the present situation of China's oil shortage of resources has determined the scarcity of aromatic hydrocarbon resource, and therefore, it is most important to seek a kind of new technology that can replace petrochemical complex to produce aromatic hydrocarbons.From the direct preparing aromatic hydrocarbon by converting of resourceful methyl alcohol,, has significant values for the shortage of alleviating aromatic hydrocarbons, the added value that improves Downstream Products of Methanol, prolongation Coal Chemical Industry and gas chemical industry's industrial chain.
CN 1880288A has introduced a kind of technology and catalyzer of methanol conversion for preparing arene; This catalyzer is carrier with the ZSM-5 molecular sieve with small crystal grains; Load active component gallium and lanthanum are that 0.1～5.0MPa, 300～460 ℃ of service temperatures, raw material liq air speed are 0.1～6.0h at working pressure
-1Catalyzed conversion is for aromatic hydrocarbons being main product under the condition, and the process refrigerated separation is with gas-phase product lower carbon number hydrocarbons and liquid product C
5 +Hydrocarbon separates, liquid product C
5 +Hydrocarbon obtains aromatic hydrocarbons and non-aromatic hydrocarbons through extracting and separating.This technological essence is the methanol conversion technique for preparing gasoline, promptly on the basis of original methanol conversion technique for preparing gasoline, through the performance modulation of catalyzer, makes that the aromaticity content in the product increases.But the used ZSM-5 molecular sieve of this technical requirements is little crystal grain, and the gas-phase product lower carbon number hydrocarbons of one section reaction get into second stage reactor continue to react the second-stage reaction product, the operational path flow process is comparatively complicated.
Summary of the invention
Technical problem to be solved by this invention is complicated and title product aromatic hydrocarbons (especially BTX) problem that selectivity is not high of the operational path flow process that exists in the prior art, and a kind of method of new methanol conversion for preparing arene is provided.This method is used for methanol conversion for preparing arene and has the high and high advantage of BTX selectivity of product of catalyst activity.
For solving the problems of the technologies described above; The technical scheme that the present invention adopts is following: a kind of method of methanol conversion for preparing arene; With methyl alcohol is raw material; Under 0.5～6.0 hour-1 condition of 320～480 ℃ of temperature of reaction, reaction pressure 0.1～3.0MPa, raw material weight hourly space velocity, raw material and catalyzer contact reacts generate aromatic hydrocarbons, and wherein used catalyzer comprises in parts by weight: a) 20～80 parts of molecular sieve carriers; With the b that carries on it) 0.5～12 part of lanthanum element or its oxide compound; C) 0.5～10 part of phosphoric or its oxide compound; D) 20～80 parts of stickers, wherein molecular sieve comprises HZSM-5 and is selected from least a mixture in HZSM-11 or the H beta-molecular sieve, HZSM-5 be selected from HZSM-11 or at least a weight ratio of H β is 0.1～10: 1.
In the technique scheme, the temperature of reaction preferable range is 360～420 ℃, and the reaction pressure preferable range is 0.5～2.0MPa, and raw material weight hourly space velocity preferable range is 1～3 hour
-1The sticker preferred version is Al
2O
3HZSM-5 be selected from HZSM-11 or at least a weight ratio preferable range of H β is 0.2～5: 1; In parts by weight, contain lanthanum element or its oxide compound preferable range in the catalyzer being 1～8 part is 1～5 part with phosphoric or its oxide compound preferable range.
The catalyzer that uses in the inventive method prepares according to following method:
(1) with the HZSM-5 of aequum and at least a and sticker that is selected from HZSM-11 or H beta-molecular sieve mix mixture I; In mixture I, add the expanding agent of gained catalyst weight 0.5～5% and the aqueous nitric acid of aequum; Pinch through mixing, moulding, drying, 500～600 ℃ of roastings be after 2～8 hours; Process support of the catalyst, wherein expanding agent is selected from the sesbania powder; (2),, process said methanol conversion for preparing arene catalyzer through dry and 450～600 ℃ of roastings 2～6 hours with the Lanthanum trinitrate of said support of the catalyst load aequum and the acid that is selected from phosphoric acid, Secondary ammonium phosphate, primary ammonium phosphate, ammonium phosphate or the salt of aequum; Wherein, phosphorated acid or salt preferably phosphoric acid ammonium dihydrogen.
Contain two kinds of cross one another pore canal system in the ZSM-5 framework of molecular sieve; (pore structure has tangible shape selectivity to mononuclear aromatics to its duct size for 0.56nm * 0.53nm, 0.55nm * 0.51nm) approaching with the kinetic diameter of aromatic hydrocarbon molecule; So be widely used in aromatization; But because the acidity of ZSM-5 is stronger, catalyzer is prone to coking deactivation, and therefore single sieve catalyst is difficult to take into account acid matter of methanol conversion for preparing arene reaction pair and the synergistic requirement of pore passage structure.The ZSM-11 molecular sieve is applied in the aromatization owing to its unique pore passage structure and acid sites, and shows higher active and stable.The H beta-molecular sieve has three-dimensional twelve-ring intersection pore passage structure, is the open system of no basket structure, helps the diffusion of molecule.ZSM-5 be selected from least a of HZSM-11 or H beta-molecular sieve and mix the intermodulation that can realize catalyst acid character and pore passage structure, thereby more help bringing into play both synergies.Adopt catalyzer of the present invention, be used for the methanol conversion for preparing arene reaction, checking and rating in the fixed-bed reactor continuously; Its methanol conversion can reach 100%, and the BTX selectivity of product can reach more than 35%, has obtained better technical effect; And technical process is merely one section reaction, and is fairly simple.
Through embodiment the present invention is done further elaboration below.
Embodiment
[embodiment 1]
The present embodiment preparation comprises: in total catalyst weight, and 2%P
2O
5, 3%La
2O
3, 30%HZSM-5,10%HZSM-11,25%H β, 30%Al
2O
3Catalyst A.
Take by weighing 30 gram HZSM-5 molecular sieves, 10 gram HZSM-11 molecular sieves, 25 gram H beta-molecular sieves, 30 gram Al
2O
3, 3.8 gram sesbania powder, it is mixed, add 42 gram mass concentration and be 5% aqueous nitric acid, fully mix and be extruded into the cylindrical of 1.5 millimeters of diameters after pinching, after 6 hours, process the support of the catalyst of 2～3 millimeters long through drying, 520 ℃ of roastings.
20 gram said catalyst carrier impregnated in 14 milliliters contain 0.63 gram La
2O
3Lanthanum nitrate aqueous solution in, in leaving standstill 24 hours, dry, 480 ℃ of roastings under the room temperature after 4 hours, process catalyst intermediate.
Above-mentioned catalyst intermediate impregnated in 14 milliliters contain 0.42 gram P
2O
5Ammonium dihydrogen phosphate aqueous solution in, in leaving standstill 24 hours, dry, 480 ℃ of roastings under the room temperature after 4 hours, process catalyst A.
390 ℃ of temperature of reaction, reaction pressure 0.3MPa, raw material weight hourly space velocity 2 hours
-1Carry out the catalyzer examination under the condition, reaction result is listed in table 2.
[embodiment 2]
The present embodiment preparation comprises: in total catalyst weight, and 2%P
2O
5, 3%La
2O
3, 30%HZSM-5,18%HZSM-11,17%H β, 30%Al
2O
3Catalyst B.
The preparation method is identical with embodiment 1, and different is to take by weighing HZSM-11 molecular sieve 18 grams, H beta-molecular sieve 17 grams.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
[embodiment 3]
The present embodiment preparation comprises: in total catalyst weight, and 2%P
2O
5, 3%La
2O
3, 30%HZSM-5,25%HZSM-11,10%H β, 30%Al
2O
3Catalyzer C.
The preparation method is identical with embodiment 1, and different is to take by weighing HZSM-11 molecular sieve 25 grams, H beta-molecular sieve 1O gram.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
[embodiment 4]
The present embodiment preparation comprises: in total catalyst weight, and 8%P
2O
5, 12%La
2O
3, 20%HZSM-5,15%HZSM-11,15%H β, 30%Al
2O
3Catalyzer D.
Take by weighing 20 gram HZSM-5 molecular sieves, 15 gram HZSM-11 molecular sieves, 15 gram H beta-molecular sieves, 30 gram Al
2O
3, 3.2 gram sesbania powder, it is mixed, add 35 gram mass concentration and be 5% aqueous nitric acid, fully mix and be extruded into the cylindrical of 1.5 millimeters of diameters after pinching, after 4 hours, process the support of the catalyst of 2～3 millimeters long through drying, 600 ℃ of roastings.
20 gram said catalyst carrier impregnated in 12 milliliters contain 3.0 gram La
2O
3Lanthanum nitrate aqueous solution in, in leaving standstill 24 hours, dry, 450 ℃ of roastings under the room temperature after 6 hours, process catalyst intermediate.
Above-mentioned catalyst intermediate impregnated in 12 milliliters contain 2.0 gram P
2O
5Ammonium dihydrogen phosphate aqueous solution in, in leaving standstill 24 hours, dry, 450 ℃ of roastings under the room temperature after 6 hours, process catalyzer D.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
[embodiment 5]
The present embodiment preparation comprises: in total catalyst weight, and 3%P
2O
5, 5%La
2O
3, 60%HZSM-5,12%HZSM-11,20%Al
2O
3Catalyzer E.
Take by weighing 60 gram HZSM-5 molecular sieves, 12 gram HZSM-11 molecular sieves, 20 gram Al
2O
3, 3.6 gram sesbania powder, it is mixed, add 45 gram mass concentration and be 5% aqueous nitric acid, fully mix and be extruded into the cylindrical of 1.5 millimeters of diameters after pinching, after 4 hours, process the support of the catalyst of 2～3 millimeters long through drying, 600 ℃ of roastings.
20 gram said catalyst carrier impregnated in 14 milliliters contain 1.09 gram La
2O
3Lanthanum nitrate aqueous solution in, in leaving standstill 24 hours, dry, 520 ℃ of roastings under the room temperature after 4 hours, process catalyst intermediate.
Above-mentioned catalyst intermediate impregnated in 14 milliliters contain 0.65 gram P
2O
5Ammonium dihydrogen phosphate aqueous solution in, in leaving standstill 4 hours, 520 ℃ roastings of 24 hours, 120 ℃ dryings under the room temperature after 4 hours, process catalyzer E.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
[embodiment 6]
The present embodiment preparation comprises: in total catalyst weight, and 5%P
2O
5, 8%La
2O
3, 17%HZSM-5,50%H β, 20%Al
2O
3Catalyzer F.
Take by weighing 17 gram HZSM-5 molecular sieves, 50 gram H beta-molecular sieves, 20 gram A1
2O
3, 3.5 gram sesbania powder, it is mixed, add 40 gram mass concentration and be 5% aqueous nitric acid, fully mix and be extruded into the cylindrical of 1.5 millimeters of diameters after pinching, after 4 hours, process the support of the catalyst of 2～3 millimeters long through drying, 600 ℃ of roastings.
20 gram said catalyst carrier impregnated in 15 milliliters contain 1.84 gram La
2O
3Lanthanum nitrate aqueous solution in, in leaving standstill 24 hours, dry, 480 ℃ of roastings under the room temperature after 4 hours, process catalyst intermediate.
Above-mentioned catalyst intermediate impregnated in 15 milliliters contain 1.15 gram P
2O
5Ammonium dihydrogen phosphate aqueous solution in, in leaving standstill 24 hours, dry, 480 ℃ of roastings under the room temperature after 4 hours, process catalyzer F.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
[comparative example 1]
The preparation of this Comparative Examples comprises: in total catalyst weight, and 5%La
2O
3, 65%HZSM-5,30%Al
2O
3Catalyzer G.
Take by weighing 65 gram HZSM-5 molecular sieves, 30 gram Al
2O
3, 3.8 gram sesbania powder, it is mixed, add 42 gram mass concentration and be 5% aqueous nitric acid, fully mix and be extruded into the cylindrical of 1.5 millimeters of diameters after pinching, after 6 hours, process the support of the catalyst of 2～3 millimeters long through drying, 520 ℃ of roastings.
20 gram said catalyst carrier impregnated in 14 milliliters contain 1.05 gram La
2O
3Lanthanum nitrate aqueous solution in, in leaving standstill 24 hours, dry, 480 ℃ of roastings under the room temperature after 4 hours, process catalyzer G.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
[comparative example 2]
The preparation of this Comparative Examples comprises: in total catalyst weight, and 2%La
2O
3, 3%Ga
2O
3, 65%HZSM-5,30%Al
2O
3Catalyzer H.
Take by weighing 65 gram HZSM-5 molecular sieves, 30 gram Al
2O
3, 3.8 gram sesbania powder, it is mixed, add 42 gram mass concentration and be 5% aqueous nitric acid, fully mix and be extruded into the cylindrical of 1.5 millimeters of diameters after pinching, after 4 hours, process the support of the catalyst of 2～3 millimeters long through drying, 600 ℃ of roastings.
20 gram said catalyst carrier impregnated in 14 milliliters contain 0.63 gram Ga
2O
3The gallium nitrate aqueous solution in, in leaving standstill 24 hours, dry, 600 ℃ of roastings under the room temperature after 2 hours, process catalyst intermediate.
Above-mentioned catalyst intermediate impregnated in 14 milliliters contain 0.42 gram La
2O
3Lanthanum nitrate aqueous solution in, in leaving standstill 24 hours, dry, 600 ℃ of roastings under the room temperature after 2 hours, process catalyzer H.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
[comparative example 3]
The preparation of this Comparative Examples comprises: in total catalyst weight, and 0.5%P
2O
5, 1%La
2O
3, 6.5%HZSM-5,6%HZSM-11,6%H β, 80%Al
2O
3Catalyst I.
Take by weighing 6.5 gram HZSM-5 molecular sieves, 6 gram HZSM-11 molecular sieves, 6 gram H beta-molecular sieves, 80 gram Al
2O
3, 4.0 gram sesbania powder, it is mixed, add 45 gram mass concentration and be 5% aqueous nitric acid, fully mix and be extruded into the cylindrical of 1.5 millimeters of diameters after pinching, after 4 hours, process the support of the catalyst of 2～3 millimeters long through drying, 600 ℃ of roastings.
20 gram said catalyst carrier impregnated in 15 milliliters contain 0.20 gram La
2O
3Lanthanum nitrate aqueous solution in, in leaving standstill 24 hours, dry, 450 ℃ of roastings under the room temperature after 6 hours, process catalyst intermediate.
Above-mentioned catalyst intermediate impregnated in 15 milliliters contain 0.10 gram P
2O
5Ammonium dihydrogen phosphate aqueous solution in, in leaving standstill 24 hours, dry, 450 ℃ of roastings under the room temperature after 6 hours, process catalyst I.
Catalyzer examination condition is identical with embodiment 1, and reaction result is listed in table 2.
Table 1 catalyst weight is formed (%)
| Example | Catalyzer | HZSM-5 | HZSM-11 | Hβ | Al 2O 3 | Ga 2O 3 | La 2O 3 | P 2O 5 |
| Embodiment 1 | A | 30 | 10 | 25 | 30 | - | 3 | 2 |
| Embodiment 2 | B | 30 | 18 | 17 | 30 | - | 3 | 2 |
| Embodiment 3 | C | 30 | 25 | 10 | 30 | - | 3 | 2 |
| Embodiment 4 | D | 20 | 15 | 15 | 30 | - | 12 | 8 |
| Embodiment 5 | E | 60 | 12 | - | 20 | - | 5 | 3 |
| Embodiment 6 | F | 17 | - | 50 | 20 | - | 8 | 5 |
| Comparative example 1 | G | 65 | - | - | 30 | - | 5 | - |
| Comparative example 2 | H | 65 | - | - | 30 | 3 | 2 | - |
| Comparative example 3 | I | 6.5 | 6 | 6 | 80 | - | 1 | 0.5 |
The methanol conversion for preparing arene reaction result (wt%) of table 2 catalyzer
[embodiment 7]
With the catalyzer of embodiment 1, it was following just to change reaction conditions: 360 ℃ of temperature of reaction, reaction pressure 2.0MPa, raw material weight hourly space velocity 3 hours
-1, all the other conditions are all with embodiment 1, and its reaction result is: methanol conversion 100.0%, it is 19.58% that hydrocarbon products weight is formed C1～C4, and aromatic hydrocarbons is 65.83%, and BTX is 24.17%.
[embodiment 8]
With the catalyzer of embodiment 1, it was following just to change reaction conditions: 420 ℃ of temperature of reaction, reaction pressure 0.1MPa, raw material weight hourly space velocity 1 hour
-1, all the other conditions are all with embodiment 1, and its reaction result is: methanol conversion 100.0%, it is 25.71% that hydrocarbon products weight is formed C1～C4, and aromatic hydrocarbons is 71.35%, and BTX is 36.83%.
[embodiment 9]
With the catalyzer of embodiment 1, it was following just to change reaction conditions: 320 ℃ of temperature of reaction, reaction pressure 3.0MPa, raw material weight hourly space velocity 6 hours
-1, all the other conditions are all with embodiment 1, and its reaction result is: methanol conversion 100.0%, it is 55.37% that hydrocarbon products weight is formed C1～C4, and aromatic hydrocarbons is 33.94%, and BTX is 22.98%.
[embodiment 10]
With the catalyzer of embodiment 1, it was following just to change reaction conditions: 480 ℃ of temperature of reaction, reaction pressure 0.1MPa, raw material weight hourly space velocity 0.5 hour
-1, all the other conditions are all with embodiment 1, and its reaction result is: methanol conversion 100.0%, it is 15.22% that hydrocarbon products weight is formed C1～C4, and aromatic hydrocarbons is 76.22%, and BTX is 40.84%.
Claims (6)
1. the method for a methanol conversion for preparing arene was a raw material with methyl alcohol, 320～480 ℃ of temperature of reaction, reaction pressure 0.1～3.0MPa, raw material weight hourly space velocity 0.5～6.0 hour
-1Under the condition, raw material and catalyzer contact reacts generate aromatic hydrocarbons (especially benzene, toluene and YLENE are referred to as BTX), and wherein used catalyzer comprises following component in parts by weight:
A) 20～80 parts of molecular sieve carriers; With carry on it
B) 0.5～12 part of lanthanum element or its oxide compound;
C) 0.5～10 part of phosphoric or its oxide compound;
D) 20～80 parts of stickers;
Wherein molecular sieve comprises HZSM-5 and is selected from least a mixture in HZSM-11 or the H beta-molecular sieve, HZSM-5 be selected from HZSM-11 or at least a weight ratio of H β is 0.1～10: 1.
2. the method for methyl alcohol system aromatic hydrocarbons according to claim 1 is characterized in that temperature of reaction is 360～420 ℃, reaction pressure 0.1～2.0MPa, raw material weight hourly space velocity 1～3 hour
-1
3. according to the method for the said methanol conversion for preparing arene of claim 1, it is characterized in that sticker is selected from Al
2O
3HZSM-5 be selected from HZSM-11 or at least a weight ratio of H β is 0.2～5: 1.
4. according to the method for the said methanol conversion for preparing arene of claim 1, it is characterized in that, contain 1～8 part of lanthanum element or its oxide compound in the catalyzer in parts by weight.
5. according to the method for the said methanol conversion for preparing arene of claim 1, it is characterized in that, contain 1～5 part of phosphoric or its oxide compound in the catalyzer in parts by weight.
6. the method for the described methanol conversion for preparing arene of claim 1, the Preparation of catalysts method may further comprise the steps successively:
(1) with the HZSM-5 of aequum and at least a and sticker that is selected from HZSM-11 or H beta-molecular sieve mix mixture I; In mixture I, add the expanding agent of gained catalyst weight 0.5～5% and the aqueous nitric acid of aequum; Pinch through mixing, moulding, drying, 500～600 ℃ of roastings be after 2～8 hours, processes support of the catalyst; Wherein expanding agent is selected from the sesbania powder;
(2),, process said methanol conversion for preparing arene catalyzer through dry and 450～600 ℃ of roastings 2～6 hours with the Lanthanum trinitrate of said support of the catalyst load aequum and the acid that is selected from phosphoric acid, Secondary ammonium phosphate, primary ammonium phosphate, ammonium phosphate or the salt of aequum.
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Application publication date: 20120314 |