CN101734989B - Method for selective toluene disproportionation and transalkylation of benzene and C9 aromatics - Google Patents
Method for selective toluene disproportionation and transalkylation of benzene and C9 aromatics Download PDFInfo
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Abstract
The invention relates to a method for selective toluene disproportionation and the transalkylation of benzene and C9 aromatics and mainly solves the problems of low paraxylene concentration in mixed xylenes, large aromatic hydrocarbon processing circulating volume, strict reaction raw material requirements and high energy consumption in the production of paraxylene in the prior art. The invention adopts a technical scheme that: in the mixed raw materials separated from a reforming unit, the C9 aromatics and a third fraction of benzene enter a benzene and C9 aromatic transalkylation technical unit to undergo a dealkylation reaction to form a section fraction of benzene, a second fraction of toluene and a second fraction of C8 aromatics; the toluene enters a selective toluene disproportionation unit to undergo a selective disproportionation reaction to form C8 aromatics and benzene homolog flow containing the paraxylene, a third fraction of C8 aromatic, a third fraction of toluene and the third fraction of benzene are obtained, and the third fraction of toluene is returned to the selective toluene disproportionation unit; and the C8 aromatics separated from the reforming unit, the second fraction of C8 aromatics and the third fraction of C8 aromatics are mixed and delivered to a paraxylene separation unit to obtain the paraxylene. According to the technical scheme, the problem is well solved, and the method can be used in the production of the paraxylene.
Description
Technical field
The present invention relates to a kind of selective disproportionation of toluene and benzene and C9 aromatic transalkylation method.
Background technology
P-Xylol is one of main basic organic of petrochemical industry, in numerous chemical production field such as chemical fibre, synthetic resins, agricultural chemicals, medicine, plastics widely purposes is arranged.Typical p-Xylol production method is that the dimethylbenzene that contains ethylbenzene of the thermodynamic(al)equilibrium that generates from the petroleum naphtha catalytic reforming is to separate or molecular sieve simulated moving bed adsorption separation (abbreviation fractionation by adsorption) technology by multistage cryogenic crystallization the C8 aronmatic, and p-Xylol is separated the close isomer mixture with it from boiling point.And for the processing of the dimethylbenzene of ortho position and a position, often take C
8A isomerization (abbreviation isomerization) technology makes it isomery and turns to p-Xylol.For increasing yield of p-xylene, utilize toluene disproportionation or toluene and carbon nine and above aromatic disproportion thereof and transalkylation (being called for short toluene disproportionation and transalkylation) reaction to generate benzene and C
8A, thereby volume increase C
8A is the operational path of effective increasing yield of p-xylene.
Up to now, in the world more typically, also the technique relevant with toluene disproportionation of comparative maturity has sixties Mo industrialized Tatoray tradition toluene disproportionation process, the MTDP of late nineteen eighties release and S-TDT technique and the TransPlus technique of releasing in recent years.Selective disproportionation of toluene is a new way of producing p-Xylol.Because toluene is at the C that can carry out selective disproportionation generation benzene and high p-Xylol concentration on the ZSM-5 of modification catalyzer
8Therefore A only needs can isolate most p-Xylol through simple once the step subzero fractionation.In recent years, along with improving constantly of catalyst performance, this technique has obtained considerable progress.Its typical process has oneself industrialized MSTDP selective disproportionation of toluene technique and the pX-Plus technique of release in recent years the late nineteen eighties.
Oneself industrialized selective disproportionation of toluene technique-MSTDP take treated ZSM-5 type mesoporous molecular sieve as the catalyst treatment methylbenzene raw material, can obtain the C of high p-Xylol concentration (85～90%, weight percent, identical except indicating below)
8The benzene of A and nitration grade.There is not yet the PX-plus technique of industrial application report, its main technique index is that the selectivity of pX reaches 90% in the dimethylbenzene under toluene conversion 30% condition, and the mol ratio of benzene and pX is 1.37.
Yet, in the technique of this class selective disproportionation of toluene, in the harshness of the simultaneous with high para-selectivity to material choice.This type of technique can only be take toluene as raw material, and C
9 +A does not have purposes in this technique, can not directly be utilized at least, causes the waste of aromatic hydrocarbon resource.In addition, this technique is a large amount of benzene of by-product also, causes the p-Xylol yield on the low side, and this is the fatal shortcoming of selective disproportionation technique.
The reactor feed of typical Tatoray technique is with toluene and C9 aromatic (C
9A) be reaction raw materials.The dimethylbenzene that is generated by Tatoray technique is to be in the isomer mixture that thermodynamic(al)equilibrium forms, and has the p-Xylol content of industrial application value generally to only have about 24% most.For the xylol this point that selective disproportionation of toluene can obtain the p-Xylol concentration about 90%, Tatoray technique is in obvious inferior position undoubtedly, but Tatoray technique is exactly that Tatoray technique can be converted into benzene and dimethylbenzene to C9A with respect to one of selective disproportionation of toluene technique very large advantage.Document take Tatoray technique as the basis has USP4341914, Chinese patent 98110859.8, USP2795629, USP3551510, Chinese patent 97106719.8 etc.The technical process that representative USP4341914 proposes is for to carry out the aromatic hydrocarbons fractionation with reformate, the toluene that obtains and C
9A enters the Tatoray technique unit and carries out disproportionation and a heatable brick bed group-transfer reaction, and resultant of reaction is toluene and C after separating
9A and part carbon ten (C
10A) circulation, benzene is as the product extraction, C8 aronmatic and the C8 aronmatic from isomerization unit enter together the pX tripping device and isolate highly purified p-Xylol product, and other C8 aronmatic isomer carries out the xylol that xylene isomerization reaction obtains being in thermodynamic(al)equilibrium again to isomerization unit.
Heavy aromatics takes off alkyl and produces C
6～C
8Aromatics process caused people's attention gradually along with the rise of selective disproportionation of toluene technique in the last few years.USP5763721 and USP5847256 have proposed respectively to be used for the catalyzer of heavy aromatics dealkylation.Wherein, USP5847256 has announced a kind of mordenite catalyst of rhenium-containing, and this catalyzer is specially adapted to transform and contains the many raw materials of ethyl, can obtain the products such as toluene, dimethylbenzene and benzene.
C
8The boiling point of each component of aromatic hydrocarbons approaches: 136.2 ℃ in ethylbenzene, 138.4 ℃ of p-Xylol, 139.1 ℃ of m-xylenes, 144.4 ℃ of o-Xylols, the o-Xylol that its mid-boiling point is the highest can be separated by rectification method, need up to a hundred theoretical stages and larger reflux ratio, the ethylbenzene that boiling point is minimum also can separate by rectification method, but much more difficult.C
8The fusing point of each component of aromatic hydrocarbons has larger gap: 13.3 ℃ of p-Xylol, o-Xylol-25.2 ℃, m-xylene-47.9 ℃, ethylbenzene-94.95 ℃.Wherein the fusing point of p-Xylol is the highest, can adopt crystallization process general p-xylene separation wherein out, and is not high such as p-Xylol concentration in the raw material, for reaching the acceptable yield of industrial production, generally adopts two sections crystallizations.USP3177255, USP3467724 at first crystallize out most p-Xylol under-80～-60 ℃ low temperature and make productive rate reach theoretical maximum, this moment crystal purity between 65～85%, is carrying out the crystallization second time after the fusing; Tc can obtain the p-Xylol of 99% above purity generally at-20～0 ℃ for the second time, and p-Xylol content is higher in the mother liquor, can return for the first time crystallized region recycle.
Utilize sorbent material to C
8The difference of each compositional selecting of aromatic hydrocarbons can be by adsorption method of separation with p-xylene separation out, after this method realizes industrialization in nineteen seventies for producing the main method of p-Xylol.USP2985589 has described the method for utilizing the simulation moving-bed separating paraxylene of adverse current; USP3686342, USP3734974, CN98810104.1 have described sorbent material that fractionation by adsorption uses and have been X or the Y zeolite of barium type or barium potassium type; USP3558732, USP3686342 use respectively toluene and p-Diethylbenzene as the desorbing agent of fractionation by adsorption.
Summary of the invention
Technical problem to be solved by this invention be in the conventional art when producing p-Xylol, exist owing to p-Xylol concentration in the xylol is low, the problem such as cause the dimethylbenzene separating unit and the isomerization unit internal circulating load is large, energy consumption is high provides a kind of new p-Xylol production method.The method is with benzene, toluene, C
8A and C
9 +A is that raw material is produced p-Xylol, improves the concentration of p-Xylol in the xylol, reduces greatly the scale of p-xylene separation unit, isomerization unit and aromatic hydrocarbons fractionation unit, thereby reduces the energy consumption of whole device.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of selective disproportionation of toluene and benzene and carbon nine transalkylation methods may further comprise the steps:
A. separate the mixing raw material that contains benzene, toluene, C8 aronmatic, carbon nine and above aromatic hydrocarbons and non-aromatics from reformer unit, isolate first strand of benzene, first strand of toluene, first burst of C8 aronmatic, carbon nine and above aromatic hydrocarbons and non-aromatics;
B.a) the isolated C9 aromatic of step and the 3rd strand of benzene enter benzene and C9 aromatic alkyl transfering process unit, carry out dealkylation under hydro condition, generate second strand of benzene, second strand of toluene and second strand of C8 aronmatic;
C. first strand of toluene and second strand of toluene enter the selective disproportionation of toluene technique unit together, under hydro condition, carry out toluene selective disproportionation reaction, generate C8 aronmatic and the benzene logistics that contains p-Xylol after the reaction, after separating, obtain the 3rd strand of C8 aronmatic, the 3rd strand of toluene and the 3rd strand of benzene, wherein the 3rd strand of toluene turns back to the selective disproportionation of toluene technique unit;
D. send into the p-xylene separation unit after first strand of C8 aronmatic, second strand of C8 aronmatic and the 3rd strand of C8 aronmatic mix, obtain the p-Xylol product, wherein the p-xylene separation unit adopts fractionation by adsorption or Crystallization Separation p-Xylol.
In technique scheme, the used catalyzer in selective disproportionation of toluene unit is the type ZSM 5 molecular sieve catalyzer, type ZSM 5 molecular sieve contains at least a metal or its oxide compound that is selected from platinum, molybdenum or the magnesium, and its consumption is 0.005～5% by weight percentage; The operational condition of selective disproportionation of toluene technique unit is as follows: reaction pressure is 1～4MPa, and temperature of reaction is 300～480 ℃, and hydrogen/hydrocarbon mol ratio is 0.5～10, and the liquid weight air speed is 0.8～8 hour
-1The used catalyzer in benzene and C9 aromatic alkyl transfering process unit is at least a molecular sieve that is selected among beta-zeolite, mordenite or the MCM-22, and the metal of bismuth-containing or its oxide compound in the catalyzer, its consumption are 0.005～5% by weight percentage; The operational condition of benzene and C9 aromatic alkyl transfering process unit is as follows: reaction pressure is 1～6MPa, and temperature of reaction is 300～600 ℃, and hydrogen/hydrocarbon mol ratio is 2～10, and weight space velocity is 0.5～3 hour
-1The p-Xylol product purity is weight concentration＞=99.8% in the p-xylene separation unit.
Among the present invention, in benzene and C9 aromatic alkyl transfering process unit, owing to use the zeolite of bismuth-containing to be catalyzer, under hydro condition, by transalkylation reaction, effectively with reaction raw materials benzene and C
9Aromatic hydrocarbons has changed into dimethylbenzene, has realized the handiness of Raw material processing, and aromatics conversion rate reaches 64.8%, and selectivity reaches 90%.And toluene selective disproportionation reaction under the effect of platiniferous ZSM-5 catalyzer, occurs in the selective disproportionation of toluene unit, generates benzene and the xylol that contains the high density p-Xylol, and p-Xylol concentration can reach 80～95%.Can find out that such operational path can allow the concentration of producing p-Xylol in the xylol that obtains significantly improve, and takes full advantage of again C
9 +The A resource has reduced the treatment scale of isomerization unit and adsorption separation unit, has effectively reduced energy consumption and facility investment scale, and has reduced production cost, has obtained preferably technique effect.
Description of drawings
Fig. 1 is the technical process of traditional p-Xylol production equipment.
Fig. 2 is the technical process of selective disproportionation of toluene of the present invention and benzene and C9 aromatic transalkylation.
I is the reformer unit deheptanizer among Fig. 1 or Fig. 2; II is the Aromatics Extractive Project unit; III is the benzene toluene separating unit after the extracting; IV is the benzenol hydrorefining unit; V is toluene disproportionation and alkyl transfering process unit; VI is the selective disproportionation technique unit; VII is benzene and C9 aromatic alkyl transfering process unit; VIII is the xylene isomerization process unit; IX is adsorption separation unit.1 is the reformation de-pentane oil, and 2 is the C that distillates from the deheptanizer cat head
7 -(comprising that benzene, toluene and carbon six carbon seven are non-aromatic), 3 carbon eight and above arene streams for the extraction of deheptanizer tower reactor, 4 for extracting benzene and the toluene logistics after non-aromatic, 5 is non-aromatic, 6 is the high purity product benzene that the benzene column overhead after the extracting is extracted, 7 is the toluene that the toluene tower cat head after the extracting is extracted, 8 C for the extraction of the toluene tower reactor after the extracting
8 +A, 9 is disproportionation and transalkylation product stream, 10 is C
8 +The C that heavy aromatics column overhead in the A fractionation unit is extracted out
9A and part C
10A, 11 is the xylol of extracting out from the benzenol hydrorefining cat head, 12 is the C that heavy aromatics Tata still is extracted out
10A, 13 is the product stream of benzene and C9 aromatic alkyl transfering process unit, 14 a small amount of toluene of separating for adsorption separation unit, the 15 pure p-Xylol of separating for adsorption separation unit, 16 for fractionation by adsorption goes out xylol behind the PX, and 17 is the C that isomerization unit deheptanizer tower reactor is discharged
8 +The A logistics, 18 logistics that contain benzene and toluene of extracting for isomerization unit deheptanizer cat head, 19 is the benzene logistics of disproportionation and transalkylation extraction, the 20 nitrated benzene of extracting for the benzene column overhead of selective disproportionation.
The technical process of tradition p-Xylol production equipment as shown in Figure 1.Enter deheptanizer I from reformation depentanizer tower bottoms 1, cat head is told carbon seven and following aromatic hydrocarbons non-aromatics logistics 2 thereof and is entered Aromatics Extractive Project unit II and carry out separating of aromatic hydrocarbons and non-aromatics, isolated non-aromatic 5 discharge, unit III is removed in benzene toluene logistics 4, the benzene column overhead of products benzene 6 after the extracting sent, and the toluene tower tower reactor of xylol 8 after the extracting extracted out and entered benzenol hydrorefining unit IV.In addition, deheptanizer tower reactor logistics 3 also enters benzenol hydrorefining unit VI, mix carbon eight logistics 11 and distillate p-xylene separation unit IX from cat head, C9 aromatic 10 and from the raw material of the isolated toluene logistics 7 of toluene tower cat head as toluene disproportionation and transalkylation II, C
10 +A logistics 12 is sent as byproduct; Disproportionation directly enters unit III with 9 of transalkylation product streams and separates; Adsorption separation unit IX isolates purpose product p-Xylol 15, and a small amount of toluene 14 returns toluene disproportionation unit VI, and other xylol 16 enters xylene isomerization unit VIII and carries out isomerization reaction, the C that isomerization unit deheptanizer tower reactor is discharged
8 +A logistics 17 is sent to benzenol hydrorefining unit IV, and the logistics that contains benzene and toluene 18 that the deheptanizer cat head is extracted is sent to the catalytic reforming unit.
The technical process of increasing yield of p-xylene in aromatic hydrocarbon production of the present invention as shown in Figure 2.Be that with the improvements of traditional technology technique of the present invention changes the toluene disproportionation process unit in the traditional technology into C9 aromatic and takes off the alkyl technique unit, in addition, increased by a cover selective disproportionation of toluene unit VI.The place that Fig. 2 is identical with Fig. 1 is no longer narrated, and the below only elaborates with regard to difference.The benzene 20 that in the technique of the present invention the former C9 aromatic 10 that is used as toluene disproportionation and transalkylation raw material and selective disproportionation unit is generated is as the raw material of benzene and C9 aromatic alkyl transfering process unit, benzene logistics 7 (comprising the toluene that the toluene brought in the raw material and reaction generate) is all as the raw material of selective disproportionation unit, product stream 9 separates with toluene tower in the benzene toluene tower unit after thing 13 flows to extracting, the logistics 8 of isolating behind benzene and the toluene is sent into benzenol hydrorefining unit IV, dimethylbenzene cat head extraction C
8 +A logistics 11, logistics 11 are sent into adsorption separation unit IX and are isolated pure p-Xylol 21.
The present invention is further illustrated below by specific embodiment, and still, scope of the present invention has more than and is limited to the scope that embodiment covers.
Embodiment
[embodiment 1]
By flow process shown in Figure 2, with C in the typical reformation de-pentane oil
6A～C
10 +Each material of hydrocarbon consist of basic data, investigate the present invention and produce the ability of p-Xylol and benzene and the treatment scale situation of each unit.Typical reformer is sent the composition distribution of aromatic hydrocarbons and the flow rate of each component that present embodiment adopts sees Table 1.
Benzene and C9 aromatic alkyl transfering process unit adopt fixed-bed reactor, and the filling bismuth-containing is 0.05% beta-zeolite catalyzer in the reactor, and reaction conditions is: 385 ℃ of temperature of reaction, pressure are 3.0MPa, and weight space velocity is 2.0 hours
-1, hydrogen/hydrocarbon mol ratio is 3.0.Aroamtic hydrocarbon raw material with after hydrogen mixes from top to bottom by beds, carry out C
9 +The dealkylation of A generates benzene, toluene and C
8A.
The selective disproportionation of toluene technique unit adopts fixed-bed reactor, and filling contains 0.05% platinum ZSM-5 molecular sieve catalyzer in the reactor, and reaction conditions is: 385 ℃ of temperature of reaction, pressure are 3.0MPa, and weight space velocity is 2.0 hours
-1, hydrogen/hydrocarbon mol ratio is 3.0.Toluene with after hydrogen mixes from top to bottom by beds, carry out toluene selective disproportionation reaction, generate the C of benzene and high p-Xylol concentration
8A.
24 grades of adsorption separation unit employings are simulation moving-bed, filling sorbent material in the moving-bed, and the fractionation by adsorption service temperature is 130 ℃.
Table 1 reformation de-pentane oil aromatic hydrocarbons forms and flow rate
| Form | Ben | Tol | C 8A | C 9A | C 10 + | ∑ |
| Form % by weight | 14.41 | 26.79 | 33.53 | 24.02 | 1.25 | 100.00 |
| Flow, kg/hr | 12673 | 23560 | 29482 | 21122 | 1095 | 87932 |
Wherein: NA is non-aromatics, and Ben is benzene, and Tol is toluene, C
8A is C8 aronmatic, C
9A is C9 aromatic, C
10 +A is carbon ten and above aromatic hydrocarbons thereof, below identical.
According to the aromatic hydrocarbons flow rate (fresh feed) in accompanying drawing 2 described technical process of the present invention and the table 1 and the operation of the parameter among the embodiment, material feeding and the discharging data of selective disproportionation of toluene unit, benzene and C9 aromatic transalkylation and isomerization unit are listed in table 2.The treatment scale of p-Xylol production equipment unit sees Table 3, and the output of product p-Xylol and benzene sees Table 4, and wherein the p-Xylol product increases by 19% with respect to Comparative Examples.
Table 2 embodiment 1 process stream table
Annotate: C
8A
*Refer to other C8 aronmatic except PX, as follows.
Table 3 embodiment 1 each cell processing scale table
| The unit title | Benzene and carbon nine transalkylation | Isomerization unit | Adsorption separation unit | The dimethylbenzene fractionation unit |
| Scale, kg/hr | 54810 | 168667 | 211965 | 252149 |
Table 4 embodiment 1 product production and purity table
| Product | P-Xylol | Benzene | Summation |
| Output, kg/hr | 58591 | 13060 | 71651 |
| Purity, % | 99.80 | 99.94 |
The result shows, uses the technology of the present invention, and with the listed aroamtic hydrocarbon raw material of table 1, the ultimate production that technique of the present invention can be produced p-Xylol and benzene is 71651 kg/hrs.The treatment scale of xylene isomerization unit, adsorption separation unit and dimethylbenzene fractionation unit has descended respectively 23%, 23% and 22%, and this has obviously reduced the design scale of device.Plant energy consumption is 21529 * 10
6Joule/ton (p-Xylol+benzene), with respect to 26579 * 10 of Comparative Examples
6Joule/ton (p-Xylol+benzene), Energy Intensity Reduction 19%.Therefore, the problem such as xylol concentration was low when patent of the present invention had overcome the production p-Xylol that exists in the conventional art, internal circulating load is large, energy consumption is high provides a kind of brand-new more economical method that is used for increasing yield of p-xylene.
[embodiment 2]
By flow process shown in Figure 2, with C in the typical reformation de-pentane oil
6A～C
10 +Each material of hydrocarbon consist of basic data, investigate the present invention and produce the ability of p-Xylol and benzene and the treatment scale situation of each unit.Typical reformer is sent the composition distribution of aromatic hydrocarbons and the flow rate of each component that present embodiment adopts sees Table 1.
Benzene and C9 aromatic alkyl transfering process unit adopt fixed-bed reactor, the Hydrogen MCM-22 zeolite catalyst of filling bismuth-containing 0.30% in the reactor, reaction conditions is: 460 ℃ of temperature of reaction, pressure are 41.0MPa, weight space velocity is 3.0 hours-1, and hydrogen/hydrocarbon mol ratio is 8.0.Aroamtic hydrocarbon raw material with after hydrogen mixes from top to bottom by beds, carry out C
9 +The dealkylation of A generates benzene, toluene and C
8A.
The selective disproportionation of toluene technique unit adopts fixed-bed reactor, filling platiniferous 0.2% and 0.5% magnesium ZSM-5 molecular sieve catalyzer in the reactor, and reaction conditions is: 450 ℃ of temperature of reaction, pressure are 6.0MPa, weight space velocity is 6.0 hours
-1, hydrogen/hydrocarbon mol ratio is 8.0.Toluene with after hydrogen mixes from top to bottom by beds, carry out toluene selective disproportionation reaction, generate the C of benzene and high p-Xylol concentration
8A.
6 grades of adsorption separation unit employings are simulation moving-bed, filling sorbent material in the moving-bed, and the fractionation by adsorption service temperature is 130 ℃.
The Crystallization Separation unit adopts suspension crystallization to separate, and Tc is 5 ℃.
Operate according to the parameter that provides in accompanying drawing 2 described technical process of the present invention and the example, the treatment scale of p-Xylol production equipment unit sees Table 5, and the output of product p-Xylol and benzene sees Table 6.
Table 5 embodiment 2 each cell processing scale table
| The unit title | Heavy aromatics takes off alkyl unit | Isomerization unit | Adsorption separation unit | The dimethylbenzene fractionation unit |
| Scale, kg/hr | 54810 | 166371 | 205929 | 235986 |
Table 6 embodiment 2 product productions and purity table
| Product | P-Xylol | Benzene | Summation |
| Output, kg/hr | 58591 | 13060 | 71651 |
| Purity, % by weight | 99.80 | 99.94 |
The result shows, uses the technology of the present invention, and with the listed aroamtic hydrocarbon raw material of table 1, the ultimate production that technique of the present invention can be produced p-Xylol and benzene is 78340 kg/hrs.The treatment scale of xylene isomerization unit, adsorption separation unit and dimethylbenzene fractionation unit has descended respectively 23%, 25% and 27%, has obviously reduced the design scale of device.Plant energy consumption is 20465 * 10
6Joule/ton (p-Xylol+benzene), with respect to 26579 * 10 of Comparative Examples
6Joule/ton (p-Xylol+benzene), Energy Intensity Reduction 23%.
[embodiment 3]
By flow process shown in Figure 2, with C in the typical reformation de-pentane oil
6A～C
10 +Each material of hydrocarbon consist of basic data, investigate the present invention and produce the ability of p-Xylol and benzene and the treatment scale situation of each unit.Typical reformer is sent the composition distribution of aromatic hydrocarbons and the flow rate of each component that present embodiment adopts sees Table 1.
Benzene and C9 aromatic alkyl transfering process unit adopt fixed-bed reactor, the h-mordenite of filling bismuth-containing 0.10% in the reactor, and reaction conditions is: 320 ℃ of temperature of reaction, pressure are 1.0MPa, weight space velocity is 0.8 hour
-1, hydrogen/hydrocarbon mol ratio is 2.0.Aroamtic hydrocarbon raw material with after hydrogen mixes from top to bottom by beds, carry out C
9 +The dealkylation of A generates benzene, toluene and C
8A.
The selective disproportionation of toluene technique unit adopts fixed-bed reactor, and filling contains 0.3% molybdenum and 0.8% magnesium ZSM-5 molecular sieve catalyzer in the reactor, and reaction conditions is: 320 ℃ of temperature of reaction, pressure are 1.0MPa, and weight space velocity is 0.8 hour
-1, hydrogen/hydrocarbon mol ratio is 1.0.Toluene with after hydrogen mixes from top to bottom by beds, carry out toluene selective disproportionation reaction, generate the C of benzene and high p-Xylol concentration
8A.
10 grades of adsorption separation unit employings are simulation moving-bed, filling sorbent material in the moving-bed, and the fractionation by adsorption service temperature is 130 ℃.
The Crystallization Separation unit adopts suspension crystallization to separate, and Tc is-15 ℃.
Operate according to the parameter that provides in accompanying drawing 2 described technical process of the present invention and the example, the treatment scale of p-Xylol production equipment unit sees Table 7, and the output of product p-Xylol and benzene sees Table 8.
Table 7 embodiment 3 each cell processing scale table
| The unit title | Heavy aromatics takes off alkyl unit | Isomerization unit | Adsorption separation unit | The Crystallization Separation unit | The dimethylbenzene fractionation unit |
| Scale, kg/hr | 54810 | 161532 | 203754 | 65101 | 245876 |
Table 8 embodiment 3 product productions and purity table
| Product | P-Xylol | Benzene | Summation |
| Output, kg/hr | 58624 | 13060 | 71684 |
| Purity, % by weight | 99.80 | 99.94 |
The result shows, uses the technology of the present invention, and with the listed aroamtic hydrocarbon raw material of table 1, the ultimate production that technique of the present invention can be produced p-Xylol and benzene is 71684 kg/hrs.The treatment scale of xylene isomerization unit, adsorption separation unit and dimethylbenzene fractionation unit has descended respectively 26%, 26% and 24%, has obviously reduced the design scale of device.Plant energy consumption is 21530 * 10
6Joule/ton (p-Xylol+benzene), with respect to 26579 * 10 of Comparative Examples
6Joule/ton (p-Xylol+benzene), Energy Intensity Reduction 19%.
[comparative example 1]
By flow process shown in Figure 1, still with typical reformation de-pentane oil C in the table 1
6A～C
10 +The flow rate of A logistics is basic data, investigates the ability that traditional Aromatic Hydrocarbon United Plant that contains toluene disproportionation and alkyl transfering process unit is as shown in Figure 1 produced p-Xylol and benzene.The material feeding of its disproportionation and transalkylation, isomerization unit and extraction situation see Table 9, and the treatment scale of each unit sees Table 10, and the output of product p-Xylol and benzene sees Table 11.
Table 9 comparative example 1 process stream table
Table 10 comparative example 1 each cell processing scale table
| The unit title | Disproportionation and transalkylation | Isomerization unit | Adsorption separation unit | The dimethylbenzene fractionation unit |
| Scale, kg/hr | 111988 | 219438 | 274572 | 323269 |
Table 11 comparative example 1 product production and purity table
| Product | P-Xylol | Benzene | Summation |
| Output, kg/hr | 54316 | 22751 | 77067 |
| Purity, % | 99.80 | 99.94 |
The result shows, traditional aromatic hydrocarbons production technique reaction aroamtic hydrocarbon raw material listed such as table 1, and the total amount that the worker has produced p-Xylol and benzene is 77067 kg/hrs, plant energy consumption is 26579 * 10
6Kilojoule/ton (p-Xylol+benzene).
Claims (1)
1. a selective disproportionation of toluene and benzene and C9 aromatic transalkylation method, enter deheptanizer I from reformation depentanizer tower bottoms (1), cat head is told carbon seven and following aromatic hydrocarbons non-aromatics logistics (2) thereof and is entered Aromatics Extractive Project unit II and carry out separating of aromatic hydrocarbons and non-aromatics, isolated non-aromatics (5) is discharged, extract the benzene toluene separating unit III after extracting is gone in benzene after the non-aromatics and toluene logistics (4), the benzene column overhead of products benzene (6) after the extracting sent, the C that the toluene tower reactor after the extracting is extracted out
8 +A (8) enters benzenol hydrorefining unit IV; In addition, carbon eight and above arene stream (3) that the deheptanizer tower reactor is extracted out also enter benzenol hydrorefining unit IV, the xylol (11) of extracting out from the benzenol hydrorefining cat head distillates adsorption separation unit IX from cat head, the toluene (7) that toluene tower cat head after the extracting is extracted is as the raw material of selective disproportionation technique unit VI, C
10 +A logistics (12) is sent as byproduct; The product stream (9) of selective disproportionation technique unit VI then directly enters benzene toluene separating unit III to be separated; Adsorption separation unit IX isolates purpose product p-Xylol (15), and a small amount of toluene (14) returns selective disproportionation technique unit VI, other xylol (16) enters xylene isomerization unit VIII and carries out isomerization reaction, the C that isomerization unit deheptanizer tower reactor is discharged
8 +A logistics (17) is sent to benzenol hydrorefining unit IV, and the logistics that contains benzene and toluene (18) that the deheptanizer cat head is extracted is sent to the catalytic reforming unit;
Wherein, the nitrated benzene (20) that the former C9 aromatic (10) that is used as selective disproportionation technique unit VI raw material and selective disproportionation technique unit VI generate is as the raw material of benzene and C9 aromatic alkyl transfering process unit VII, toluene tower among the benzene toluene tower unit III of the product stream (13) of the product stream (9) of selective disproportionation technique unit VI and benzene and C9 aromatic alkyl transfering process unit VII after the extracting separates the C that the toluene tower reactor after the extracting is extracted out
8 +A (8) sends into benzenol hydrorefining unit IV, and dimethylbenzene cat head extraction xylol (11) is sent into adsorption separation unit IX and isolated pure p-Xylol (21);
According to above-mentioned flow process, with C in the typical reformation de-pentane oil
6A～C
10 +Each material of hydrocarbon consist of basic data, investigate the present invention and produce the ability of p-Xylol and benzene and the treatment scale situation of each unit, C in the described typical reformation de-pentane oil
6A～C
10 +Composition and the flow rate of each material of hydrocarbon are as follows:
Benzene (Ben): 14.41 % by weight, flow are 12673 kg/hrs;
Toluene (Tol): 26.79 % by weight, flow are 23560 kg/hrs;
C8 aronmatic (C
8A): 33.53 % by weight, flow are 29482 kg/hrs;
C9 aromatic (C
9A): 24.02 % by weight, flow are 21122 kg/hrs;
Carbon ten and above aromatic hydrocarbons (C thereof
10 +): 1.25 % by weight, flow are 1095 kg/hrs;
Benzene and C9 aromatic alkyl transfering process unit adopt fixed-bed reactor, the Hydrogen MCM-22 zeolite catalyst of filling bismuth-containing 0.30% in the reactor, and reaction conditions is: 460 ℃ of temperature of reaction, pressure are 41.0MPa, weight space velocity is 3.0 hours
-1, hydrogen/hydrocarbon mol ratio is 8.0; Aroamtic hydrocarbon raw material with after hydrogen mixes from top to bottom by beds, carry out C
9 +The dealkylation of A generates benzene, toluene and C
8A;
The selective disproportionation of toluene technique unit adopts fixed-bed reactor, filling platiniferous 0.2% and 0.5% magnesium ZSM-5 molecular sieve catalyzer in the reactor, and reaction conditions is: 450 ℃ of temperature of reaction, pressure are 6.0MPa, weight space velocity is 6.0 hours
-1, hydrogen/hydrocarbon mol ratio is 8.0; Toluene with after hydrogen mixes from top to bottom by beds, carry out toluene selective disproportionation reaction, generate the C of benzene and high p-Xylol concentration
8A;
6 grades of adsorption separation unit employings are simulation moving-bed, filling sorbent material in the moving-bed, and the fractionation by adsorption service temperature is 130 ℃;
The Crystallization Separation unit adopts suspension crystallization to separate, and Tc is 5 ℃;
The treatment scale of p-Xylol production equipment unit is as follows:
Heavy aromatics takes off alkyl unit: 54810 kg/hrs;
Isomerization unit: 166371 kg/hrs;
Adsorption separation unit: 205929 kg/hrs;
Dimethylbenzene fractionation unit: 235986 kg/hrs;
The output of product p-Xylol and benzene is respectively 58591 kg/hrs and 13060 kg/hrs, and summation is 71651 kg/hrs, and purity is respectively 99.80 % by weight and 99.94 % by weight.
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| US9090523B1 (en) | 2014-03-03 | 2015-07-28 | Uop Llc | Process for flushing top and bottom heads of a vessel |
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| CN104107717B (en) * | 2013-04-16 | 2016-12-28 | 中国石油化工股份有限公司 | Improve toluene disproportionation catalyst of dimethylbenzene selective and application thereof |
| CN103845915B (en) * | 2014-02-15 | 2015-06-17 | 中山大学 | Multi-stage flash evaporation separation equipment of toluene disproportionation reaction effluent and separation method thereof |
| CN109803944A (en) * | 2016-10-04 | 2019-05-24 | 埃克森美孚化学专利公司 | The disproportionation and transalkylation of heavy arene |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1340489A (en) * | 2000-08-29 | 2002-03-20 | 中国石油化工集团公司 | Process for preparing p-xylene |
| CN1443736A (en) * | 2002-03-13 | 2003-09-24 | 中国石油化工股份有限公司 | Benzene and C9 and more than that arene transalkylation method |
| CN1506341A (en) * | 2002-12-11 | 2004-06-23 | 中国石油化工股份有限公司 | Transalkylation process between benzene and C9 arene |
| CN1566046A (en) * | 2003-07-09 | 2005-01-19 | 中国石油化工股份有限公司 | Toluene selective disproportionation and carbon 9 and above arene dealkytation method |
| CN101091919A (en) * | 2006-06-21 | 2007-12-26 | 中国石油化工股份有限公司 | Catalyst transference of polyalkylbenzene alkyl |
-
2008
- 2008-11-21 CN CN2008100439761A patent/CN101734989B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1340489A (en) * | 2000-08-29 | 2002-03-20 | 中国石油化工集团公司 | Process for preparing p-xylene |
| CN1443736A (en) * | 2002-03-13 | 2003-09-24 | 中国石油化工股份有限公司 | Benzene and C9 and more than that arene transalkylation method |
| CN1506341A (en) * | 2002-12-11 | 2004-06-23 | 中国石油化工股份有限公司 | Transalkylation process between benzene and C9 arene |
| CN1566046A (en) * | 2003-07-09 | 2005-01-19 | 中国石油化工股份有限公司 | Toluene selective disproportionation and carbon 9 and above arene dealkytation method |
| CN101091919A (en) * | 2006-06-21 | 2007-12-26 | 中国石油化工股份有限公司 | Catalyst transference of polyalkylbenzene alkyl |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9090523B1 (en) | 2014-03-03 | 2015-07-28 | Uop Llc | Process for flushing top and bottom heads of a vessel |
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