CN1042529C - Aromatization process for splitting SC-cut - Google Patents
Aromatization process for splitting SC-cut Download PDFInfo
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- CN1042529C CN1042529C CN94111416A CN94111416A CN1042529C CN 1042529 C CN1042529 C CN 1042529C CN 94111416 A CN94111416 A CN 94111416A CN 94111416 A CN94111416 A CN 94111416A CN 1042529 C CN1042529 C CN 1042529C
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- 238000005899 aromatization reaction Methods 0.000 title claims description 20
- 238000000034 method Methods 0.000 title claims description 15
- 230000008569 process Effects 0.000 title claims description 12
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 42
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000002994 raw material Substances 0.000 claims abstract description 26
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 25
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000005516 engineering process Methods 0.000 claims abstract description 20
- 239000000203 mixture Substances 0.000 claims abstract description 19
- 239000000463 material Substances 0.000 claims abstract description 18
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 239000008096 xylene Substances 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 239000002808 molecular sieve Substances 0.000 claims abstract description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 6
- 239000007791 liquid phase Substances 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 46
- 238000005336 cracking Methods 0.000 claims description 34
- 230000008929 regeneration Effects 0.000 claims description 19
- 238000011069 regeneration method Methods 0.000 claims description 19
- 238000004821 distillation Methods 0.000 claims description 7
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 5
- 239000003209 petroleum derivative Substances 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- 238000010792 warming Methods 0.000 claims description 4
- 238000009834 vaporization Methods 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 2
- 239000011248 coating agent Substances 0.000 claims description 2
- 238000000576 coating method Methods 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 239000001301 oxygen Substances 0.000 claims description 2
- 229910052760 oxygen Inorganic materials 0.000 claims description 2
- -1 xylene aromatic hydrocarbon Chemical class 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 claims 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 16
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- 229930195733 hydrocarbon Natural products 0.000 abstract description 7
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 7
- 239000000446 fuel Substances 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 3
- 239000003208 petroleum Substances 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract 1
- 239000000969 carrier Substances 0.000 abstract 1
- 229910052681 coesite Inorganic materials 0.000 abstract 1
- 229910052593 corundum Inorganic materials 0.000 abstract 1
- 229910052906 cristobalite Inorganic materials 0.000 abstract 1
- 239000000377 silicon dioxide Substances 0.000 abstract 1
- 235000012239 silicon dioxide Nutrition 0.000 abstract 1
- 229910052682 stishovite Inorganic materials 0.000 abstract 1
- 229910052905 tridymite Inorganic materials 0.000 abstract 1
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract 1
- 239000000047 product Substances 0.000 description 12
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical compound CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 6
- 125000003118 aryl group Chemical group 0.000 description 6
- LBPGAOJVQOCVLO-UHFFFAOYSA-N benzene ethylbenzene toluene Chemical compound C1=CC=CC=C1.CC1=CC=CC=C1.CCC1=CC=CC=C1 LBPGAOJVQOCVLO-UHFFFAOYSA-N 0.000 description 6
- IVSZLXZYQVIEFR-UHFFFAOYSA-N m-xylene Chemical group CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 6
- 239000012495 reaction gas Substances 0.000 description 6
- 238000003860 storage Methods 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 5
- 239000003915 liquefied petroleum gas Substances 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000004044 response Effects 0.000 description 4
- 239000006200 vaporizer Substances 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
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- 229910001385 heavy metal Inorganic materials 0.000 description 1
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- 238000011068 loading method Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 1
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- 238000000197 pyrolysis Methods 0.000 description 1
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- 239000010959 steel Substances 0.000 description 1
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Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention provides a technology for aromatizing petroleum hydrocarbons and a fixed bed reactor thereof. In the aromatizing technology of the present invention, cracked C5 fractions are used as raw materials and are heated and vaporized by a heating furnace, the heating temperature is from 350 to 500 DEG C, gas materials after the heating enter the fixed bed reactor for reaction, materials which are discharged from the reactor are condensed and cooled, liquid phase parts of the materials mainly comprise mixtures of benzene, toluene and xylene, the liquid yield of the reaction materials is from 63 to 67%(wt%), and aromatic hydrocarbon products of benzene, toluene, xylene, etc., are respectively obtained through the separation of a rectification system. Shape selective catalysts are filled in the fixed bed reactor, the catalysts use ZSM-5 type molecular sieves as carriers and comprise active components of Al2O3, SiO2, Zn, Na, Ge, etc. When the technology of the present invention is used, the cracked C5 fractions can be directly used as fuels, and can be comprehensively utilized, the production cost is greatly lowered, the use added value of the cracked C5 fractions is enhanced, unnecessary waste is reduced, and therefore, the technology of the present invention has good popularization prospects.
Description
The present invention relates to the cracking hydrocarbon oil of petroleum hydrocarbon, be meant by product cracking C especially cracking hydrocarbon oil
5(being carbon five, down together) cut carries out aromizing, and adopting type ZSM 5 molecular sieve is that carrier is with Al
2O
3, SiO
2, Zn, Na, Ge etc. are the type of the selecting catalyzer of active principle, carry out reaction such as deoxidation, aromatization and obtain the technology and the conversion unit thereof of aromatic hydrocarbons.
Existing to cracking hydrocarbon oil by product cracking C
5The utilization of cut, the domestic overwhelming majority use that acts as a fuel is not abroad seen about cracking C as yet yet
5The report of aromizing industrialness production application.Though existing lower carbon number hydrocarbons (C
2～C
4) report of technology of aromatization technology, but it can only use Sweet natural gas and refinery gas to be raw material, can't solve to use cracking C
5Cut is the relevant Technology of raw material production aromatic hydrocarbons.Thereby both at home and abroad to this refining of petroleum by product cracking C
5The comprehensive utilization of cut does not all have the fixed production model as yet.
It is a kind of with cracking hydrocarbon oil by product cracking C that purpose of the present invention just is to provide
5Cut is that raw material carries out aromizing and is suitable for the Technology and the conversion unit thereof of suitability for industrialized production, and this production technique is with cheap cracking C
5Cut is aromatic hydrocarbon products such as raw material production benzene,toluene,xylene, goes back by-product ethene, propylene and liquefied petroleum gas (LPG) simultaneously, makes C
5Cut is able to sufficient comprehensive utilization.
Production technique of the present invention is with cracking C
5Cut is a raw material, and through vaporizer, process furnace heating vaporization, the Heating temperature scope is 350～500 ℃ to raw material earlier; Heating back gas material enters the fixed-bed reactor reaction, is filled with shape-selective catalyst in the reactor, and catalyzer is carrier with the type ZSM 5 molecular sieve, with Al
2O
3, SiO
2, Zn, Na, Ge etc. be active principle; Reaction pressure 0.05～0.3MPa, air speed 0.3～0.8h
-1The reaction mass that goes out reactor is after the condensation cooling, gas phase part is by recovery system separating and reclaiming ethylene, propylene and the liquefied petroleum gas (LPG) of sloughing heavy constituent, liquid phase part mainly is the benzene,toluene,xylene mixture, obtains aromatic hydrocarbon products such as benzene,toluene,xylene after separating through distillation system respectively; For cracking C 5 fraction raw material, the gas yield of reaction mass is 30-33% (wt%), and liquid yield is 63-67% (wt%).The raffinate of rectifying discharging is mainly the C9 component, offers Subscriber Unit as the C9 solvent oil.
Cracking C
5The technological process of aromizing, some principal reactions of generation are as follows: (not comprising total overall reaction)
(1) long chain alkane generation scission reaction in the raw material:
(2) alkane in the raw material carries out dehydrogenation reaction under catalyst action:
(3) oligomerisation takes place in alkene under catalyst action:
(4) oligopolymer dehydrocyclization under catalyst acid central role becomes aromatic hydrocarbons:
Cracking C
5The key of technology of aromatization is to have adopted fixed-bed reactor and selected with Al
2O
3, SiO
2, Zn, Na, Ge etc. be the modified ZSM-5 type molecular sieve catalyst of active principle.Fixed-bed reactor are cylinder mode, and gaseous phase materials enters reactor by top and leaves from its underpart.The entry site of gas phase is provided with the gas inlet sparger, and outlet at bottom is provided with the cover cap and takes out of with gas to prevent catalyzer.The both sides, top of reactor are provided with the catalyzer loading port, and two bottom sides has catalyzer to unload outlet.The catalyzer close packing is in reactor, for the heat that reaction is produced is in time taken out of, be provided with heat collector in the built-up type in the reactor, reached the purpose that reclaims heat energy simultaneously by making steam superheating can in time shift out reaction heat, catalyst regeneration operates in the fixed-bed reactor and carries out, realize internal regeneration, significantly reduced the wearing and tearing of catalyzer.
Of the present invention with cracking C
5Cut is the technology of raw material production aromatic hydrocarbons, also pyrolysis gasoline, condensation wet goods can be replenished as raw material, and its raw material scope of application is wider, is not limited to cracking C
5Cut.
Advantage of the present invention just is to provide a kind of cheap cracking C that uses
5Cut is the technology and the reactor thereof of raw material production aromatic hydrocarbons, makes cracking C
5The use of cut also can be fully utilized except that directly acting as a fuel, and greatly reduces production cost, has improved it and has used added value, has reduced unnecessary waste.And this technology do not have residual liquid discharge, and production process can not work the mischief to environment substantially.Owing to adopted reclaiming process in fixed-bed reactor and the catalyst body, make simple to operately, catalyst abrasion is little, and the steam superheating mode by heat collector in the reactor not only can in time shift out reaction heat but also has reclaimed heat energy.Therefore adopt Technology of the present invention to produce aromatic hydrocarbons and have promotion prospect preferably.
Below in conjunction with accompanying drawing technology of the present invention and reactor thereof are further described.
Fig. 1 is a process flow diagram of the present invention;
Fig. 2 is a fixed-bed reactor structural representation of the present invention.
With reference to Fig. 1, technological process of the present invention is divided into aromatization and separates two parts with rectifying, equipment comprises regeneration gas gas holder [1], regeneration gas heat exchanger [2], regeneration gas cooler [3], regeneration gas separator [4], regeneration gas compressor [5], C5 storage tank [7], vaporizer [9], heating furnace [10], fixed bed reactors [12], drum [13], waste heat boiler [14], reactor heat exchanger [15], reaction gas cooler [16], exhaust gas cooler [17], gas-liquid separator [18], reaction gas gas holder [19], reactant liquor storage tank [21], feed exchanger [22], tower reboiler [23], non-aromatic tower [24], overhead condensation cooler [25], backflow cylinder [26], benzene rectifying column [27], toluene rectifying column [29], xylene distillation tower [31] etc. Such as figure, C5Feedstock enters C through storage tank import [6]5Storage tank [7], steam [8] is used for the C in the vaporizer [9]5The vaporization of cut, soft water [11] are removed drum [13] after entering heating furnace [10], and the reacting gas that goes out fixed bed reactors [12] is through reaction gas gas holder [19] the body separator [20] that degass. Liquid phase material obtains respectively benzaldehyde product [28], toluene product [30], dimethylbenzene product [32] through benzene rectifying column [27], toluene rectifying column [29], xylene distillation tower [31], pumped vacuum systems [33] is connected 31 with toluene rectifying column [29] with the xylene distillation tower respectively] be connected, discharge C at the bottom of xylene distillation tower [31] tower9Cut and tar [34].
Because the catalyst single pass life is about 24-50 hour, general many group gasifiers, heating furnace, fixed bed reactors parallel-connection flow, the needs that hocket to adapt to fixed bed reactors [12] aromatization and catalyst regeneration of adopting of the aromatization part of technique of the present invention. When carrying out aromatization, by feed pump with C5Cut is from C5Storage tank [7] is delivered to vaporizer [9], material is through vaporizing and being raised to about 160 ℃, enter again heating furnace [10] and be warming up to 350-500 ℃, heating furnace is made fuel with methane gas, gas material after the heating enters fixed bed reactors [12], under the effect of modified molecular screen shape-selective catalyst series reaction occurs. The optimal reaction temperature of fixed bed reactors [12] control is 350-400 ℃, and optimum response pressure is 0.05-0.3MPa, air speed 0.3-0.8h-1 The reacting gas temperature that goes out fixed bed reactors [12] is 450-550 ℃, and it is cooled to about 350 ℃ through waste heat boiler [14] and further is cooled to about 250 ℃ by reaction gas heat exchanger [15], then enters reaction gas cooler [16]. Behind condensing cooling, its condensate liquid is the mixture of benzene,toluene,xylene etc., by being pumped into reactant liquor storage tank [21] as the rectifying charging; Its tail gas is the mixture of ethene, propylene, liquefied petroleum gas etc., is sent to reaction gas gas holder [19] after exhaust gas cooler [17] cooling. When carrying out catalyst regeneration, the aromatization process stops, oxygen content in the regeneration gas gas holder [1] is delivered to regeneration gas heat exchanger [2] heat exchange less than 2% nitrogen through regeneration gas compressor [5] supercharging be warming up to 250 ℃, system's controlled pressure is that normal pressure is to 0.5MPa, then be warming up to through heating furnace [10] and enter fixed bed reactors [12] about 450-550 ℃ again, carbon deposit makes catalyst regeneration on the burning-off catalyst coating. The gas that burns that goes out fixed bed reactors [12] is cooled to 350 ℃ after regeneration gas heat exchanger [2] heat exchange, heated simultaneously the regeneration gas that enters fixed bed reactors [12], burn gas after regeneration gas cooler [3] further is cooled to less than 50 ℃, begin again a new round by regeneration gas compressor [5] behind the additional part air and burn circulation. The recovery time of catalyst and aromatization time are equal to substantially. Through the liquid phase material mixtures such as benzene,toluene,xylene that aromatisation obtains, its " triphen " content accounts for more than 90% (wt%), and the distillation and separation method by routine obtains respectively the aromatic hydrocarbon products such as benzene,toluene,xylene, and the raffinate of discharge is with C9Cut is main, as C9Solvent naphtha offers Subscriber Unit and uses. Adopt the basic three-waste free discharge of technology of aromatization of the present invention, heating fume emission after measured CO content was less than or equal to for 0.2% (meeting discharge standard); Heavy metal free pollutes in the discarded catalyst, concentrates after calcining and buries processing.
With reference to Fig. 2, fixed bed reactors are cylinder mode, ratio of height to diameter: 1.9: be mainly the formations such as cylindrical shell, material inlet, material outlet, catalyst inlet [1], [2], catalyst outlet [3], [4], gas inlet distributor [5], gas vent cover cap [6], interior heat collector [7]. Top gas inlet distributor [5] is frustum of a cone multilayer conical distribution structure, by 4 layers of descending cast gas access passage Uniform Dispersion entrance gas phase, has effectively guaranteed the even distribution of gas. Bottom gas vent cover cap [6] is cylindrical structure, and its diameter is D9600, and its top is by cover closure, and wall has bar hole, and gas vent cover cap [6] major function is to prevent taking out of of catalyst. Interior heat collector [7] adopts the seamless steel pipe of Φ 57 * 3.5, is installed in the cylindrical shell inner ring distance Φ 600 such as figure minute three circles; Centre circle spacing Φ 1200; Outer ring spacing Φ 1700. Steam enters coil pipe by the reactor shell lower end, and upper recircling to the coil pipe top and descending exports from the lower end opposite side at last. The interior heat collector form also can adopt shell and tube and other forms. Can in time shift out again recyclable heat energy of reaction heat by interior heat collector [7].
Below be embodiments of the invention.
Example 1, cracking C
5Production contrast under the differential responses temperature
Year is handled cracking C
510,000 tons of cuts adopt fixed-bed reactor nominal diameter Dg2200mm, volume 12M
3Catalyzer is with Al
2O
3, SiO
2, Zn, Na, Ge etc. are carrier for active principle with ZMC-5 type molecular sieve, useful volume 8.5M
3The operation air speed is 0.3-0.8h
-1
1, cracking C
5The raw material composition is listed in table 1;
2, the product composition under the differential responses temperature is listed in table 2.
Table 1 cracking C
5The composition of raw material
| Component | Cracking C 5Cut | Benzene | Toluene | Ethylbenzene | P-Xylol | M-xylene | O-Xylol | C 5Aromatic hydrocarbons |
| Content (wt%) | 89.673 | 9.069 | 0.415 | - | 0.532 | - | - | 0.321 |
Product under the table 2 differential responses temperature is formed (wt%)
| Temperature of reaction ℃ | Gas composition | Aromatic hydrocarbons is formed | Total aromatic hydrocarbons | |||||||||||
| C 1° | C 2 - | C 2° | C 3 - | C 3° | C 4 | Benzene | Toluene | Ethylbenzene | P-Xylol | M-xylene | O-Xylol | C9 aromatic | ||
| 560 | 4.36 | 5.36 | 6.23 | 2.90 | 8.68 | 4.28 | 15.6 | 30.81 | 0.9 | 3.48 | 8.27 | 3.74 | 1.56 | 64.36 |
| 520 | 3.50 | 6.32 | 6.33 | 4.84 | 7.29 | 3.71 | 17.33 | 31.08 | 1.1 | 3.26 | 7.81 | 3.69 | 2.04 | 66.31 |
| 480 | 2.33 | 5.85 | 4.91 | 5.06 | 6.14 | 4.0 | 19.84 | 27.76 | 2.44 | 3.71 | 7.14 | 3.29 | 3.73 | 67.91 |
Example 2: use different material to realize the contrast that aromizing is produced
Reaction control temperature 350-500 ℃, use cracking C respectively
5, cracking C
5Mixing light oil and light oil is raw material, and other conditions are with example 1.
1, different raw material compositions are listed in table 3;
2, the product of different material composition is listed in table 4.
The different raw material of table 3 is formed (wt%)
| Name of material | Form | |||||||
| Non-aromatics | Benzene | Toluene | Ethylbenzene | P-Xylol | M-xylene | O-Xylol | C9 aromatic | |
| Cracking C 5 | 99.109 | - | - | - | - | - | - | 0.326 |
| Cracking C 5Mix light oil | 47.638 | 32.028 | 15.690 | 0.274 | - | 1.477 | 2.89 | - |
| Light oil | 18.254 | 46.384 | 24.817 | 0.576 | 0.896 | 1.941 | 0.835 | 6.35 |
The product of table 4 different material is formed (wt%)
| Name of material | Gas composition | Aromatic hydrocarbons is formed | Total aromatic hydrocarbons | |||||||||||
| C 1° | C 2 - | C 2° | C 3 - | C 3° | C 4 | Benzene | Toluene | Ethylbenzene | P-Xylol | M-xylene | O-Xylol | C9 aromatic | ||
| Cracking C 5 | 3.96 | 3.26 | 6.09 | 2.74 | 11.64 | 4.22 | 14.07 | 31.85 | 1.39 | 3.95 | 8.74 | 3.91 | 0.23 | 64.14 |
| Cracking C 5Mix light oil | 2.02 | 2.63 | 5.15 | 1.87 | 5.81 | 1.37 | 28.85 | 31.62 | 2.66 | 2.95 | 5.91 | 2.77 | 1.31 | 76.07 |
| Light oil | 1.07 | 0.76 | 2.07 | 0.48 | 2.94 | 0.34 | 49.59 | 29.54 | 2.69 | 1.44 | 3.33 | 1.79 | 0.59 | 88.97 |
Example 3 is that raw material uses different catalyzer to carry out the contrast of aromizing with light oil
Reaction control temperature is 350-450 ℃, and other conditions are with example 1.
1, the composition of light oil raw material is listed in table 5; 2, the product of different catalyzer composition is listed in table 6.
The composition (wt%) of table 5 light oil raw material
| Component | Non-aromatics | Benzene | Toluene | Ethylbenzene | P-Xylol | M-xylene | O-Xylol | C9 aromatic |
| Content | 16.847 | 46.901 | 24.448 | 0.514 | 0.977 | 2.204 | 1.048 | 4.86 |
The product of the catalyzer that table 6 is different is formed (wt%)
| Catalyzer research institute title | Gas composition | Aromatic hydrocarbons is formed | Total aromatic hydrocarbons | |||||||||||
| C 1° | C 2 - | C 2° | C 3 - | C 3° | C 4 | Benzene | Toluene | Ethylbenzene | P-Xylol | M-xylene | O-Xylol | C9 aromatic | ||
| Nankai University | 0.66 | 0.91 | 1.02 | 0.73 | 1.91 | 1.02 | 51.56 | 29.89 | 3.04 | 1.57 | 2.91 | 1.37 | 1.64 | 91.98 |
| Kingsoft, Shanghai general petrochemicals factory | 0.98 | 3.24 | 1.19 | 2.68 | 2.01 | 1.74 | 45.53 | 26.99 | 3.35 | 1.67 | 3.87 | 2.49 | 1.43 | 85.33 |
| Huadong Chemical College | 0.47 | 3.16 | 0.26 | 3.93 | 0.95 | 1.99 | 48.05 | 27.71 | 2.18 | 1.12 | 2.40 | 2.12 | 2.81 | 86.39 |
Claims (4)
1, a kind of petroleum hydrocarbon technology of aromatization is characterized in that:
A. with cracking C
5Cut is a raw material, through process furnace heating vaporization, Heating temperature is 350-550 ℃, heating back gas material enters the fixed-bed reactor reaction, the material liquid phase part after the condensation cooling that goes out reactor mainly is the benzene,toluene,xylene mixture, the liquid yield of reaction mass is 63-67% (wt%), obtains the benzene,toluene,xylene aromatic hydrocarbon product respectively after distillation system separates;
B. load shape-selective catalyst in the fixed-bed reactor, catalyzer is a carrier with the type ZSM 5 molecular sieve, with Al
2O
3, SiO
2, Zn, Na, Ge be active principle.
2, according to claim 1 with cracking C
5Cut is the petroleum hydrocarbon technology of aromatization of raw material, it is characterized in that aromatization partly adopts the flow process of many group gasifiers, process furnace, fixed-bed reactor parallel connection, and aromatization and catalyst regeneration hocket; With oxygen level less than the compressed machine supercharging of 2% nitrogen, Controlling System pressure is that normal pressure is to 0.5MPa, be warming up to about 450-550 ℃ through process furnace and enter fixed-bed reactor, burning-off catalyst coating carbon deposit makes catalyst regeneration, and regenerative operation time and aromatization time are equal to substantially.
3, according to claim 1 with cracking C
5Cut is the petroleum hydrocarbon technology of aromatization of raw material, and the reaction control temperature that it is characterized in that fixed-bed reactor is 350-400 ℃; Reaction pressure is 0.05-0.3MPa, air speed 0.3-0.8h
-1
4, a kind of cracking C as claimed in claim 1
5Cut is the employed fixed-bed reactor of petroleum hydrocarbon technology of aromatization of raw material, it is characterized in that its gas phase entry site is provided with gas inlet sparger [5], and outlet at bottom is provided with pneumatic outlet cover cap [6], and is provided with interior heat collector [7] in reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94111416A CN1042529C (en) | 1994-08-17 | 1994-08-17 | Aromatization process for splitting SC-cut |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94111416A CN1042529C (en) | 1994-08-17 | 1994-08-17 | Aromatization process for splitting SC-cut |
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| Publication Number | Publication Date |
|---|---|
| CN1111227A CN1111227A (en) | 1995-11-08 |
| CN1042529C true CN1042529C (en) | 1999-03-17 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN94111416A Expired - Fee Related CN1042529C (en) | 1994-08-17 | 1994-08-17 | Aromatization process for splitting SC-cut |
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| CN (1) | CN1042529C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102151523B (en) * | 2011-03-14 | 2013-06-19 | 高玉玲 | Aromatization reactor |
| CN111777481B (en) * | 2020-07-17 | 2023-04-11 | 青岛大学 | Novel process for producing triphenyl by utilizing aromatization of cracking carbon penta |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4417083A (en) * | 1980-05-09 | 1983-11-22 | Elf France | Process for the dehydrocyclization of paraffins at low pressure |
| WO1990006907A1 (en) * | 1988-12-12 | 1990-06-28 | Linde Aktiengesellschaft | Process and catalyst for dehydration or dehydrocyclization of hydrocarbons |
| CN1048379A (en) * | 1989-06-28 | 1991-01-09 | 抚顺石油学院 | Technology of aromatization of low carbon hydrocarbon |
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1994
- 1994-08-17 CN CN94111416A patent/CN1042529C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4417083A (en) * | 1980-05-09 | 1983-11-22 | Elf France | Process for the dehydrocyclization of paraffins at low pressure |
| WO1990006907A1 (en) * | 1988-12-12 | 1990-06-28 | Linde Aktiengesellschaft | Process and catalyst for dehydration or dehydrocyclization of hydrocarbons |
| CN1048379A (en) * | 1989-06-28 | 1991-01-09 | 抚顺石油学院 | Technology of aromatization of low carbon hydrocarbon |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1111227A (en) | 1995-11-08 |
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