CN201620141U - Reforming system for fecundation of aromatic hydrocarbon and solvent oil with naphtha - Google Patents
Reforming system for fecundation of aromatic hydrocarbon and solvent oil with naphtha Download PDFInfo
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- CN201620141U CN201620141U CN2009202783763U CN200920278376U CN201620141U CN 201620141 U CN201620141 U CN 201620141U CN 2009202783763 U CN2009202783763 U CN 2009202783763U CN 200920278376 U CN200920278376 U CN 200920278376U CN 201620141 U CN201620141 U CN 201620141U
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- 239000002904 solvent Substances 0.000 title claims abstract description 41
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 24
- 238000002407 reforming Methods 0.000 title claims abstract description 23
- 238000000605 extraction Methods 0.000 claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 claims abstract description 45
- 238000011084 recovery Methods 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 9
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- 239000003381 stabilizer Substances 0.000 claims description 17
- 230000006835 compression Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 23
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 23
- 239000001257 hydrogen Substances 0.000 abstract description 23
- 239000007788 liquid Substances 0.000 abstract description 10
- 238000005406 washing Methods 0.000 abstract description 4
- 230000006641 stabilisation Effects 0.000 abstract 1
- 238000011105 stabilization Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 103
- 238000000034 method Methods 0.000 description 39
- 238000009835 boiling Methods 0.000 description 22
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 17
- 239000003054 catalyst Substances 0.000 description 14
- 239000000047 product Substances 0.000 description 14
- 239000005864 Sulphur Substances 0.000 description 13
- 238000010992 reflux Methods 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 10
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 9
- 239000007795 chemical reaction product Substances 0.000 description 8
- 239000003502 gasoline Substances 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000001833 catalytic reforming Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- 235000019628 coolness Nutrition 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 238000012545 processing Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- 150000001335 aliphatic alkanes Chemical class 0.000 description 4
- 238000003556 assay Methods 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 3
- 239000003209 petroleum derivative Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000004440 column chromatography Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 229910001648 diaspore Inorganic materials 0.000 description 2
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 229910052702 rhenium Inorganic materials 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000002795 fluorescence method Methods 0.000 description 1
- 239000003269 fluorescent indicator Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009616 inductively coupled plasma Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000003918 potentiometric titration Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- HYERJXDYFLQTGF-UHFFFAOYSA-N rhenium Chemical compound [Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re] HYERJXDYFLQTGF-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000007655 standard test method Methods 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- UWHCKJMYHZGTIT-UHFFFAOYSA-N tetraethylene glycol Chemical compound OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
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Abstract
The utility model discloses a reforming system for fecundation of aromatic hydrocarbon and solvent oil with naphtha, which comprises a heating device and a reaction device connected with the heating device. The reforming system is characterized in that the reaction device is divided into two parts, a first reaction device and/or a second reaction device is/are connected with a raffinate cutting system through a high-pressure separation device, a stabilization tower system, an extraction system, a recovery system and a washing system, and simultaneously the raffinate cutting system is connected with a third reaction device and/or a fourth reaction device. The utility model has the advantage of greatly improving the treatment capability, the liquid yield, the yield of the aromatic hydrocarbon, the yield of various kinds of solvent oil and the hydrogen output.
Description
Technical field
The utility model relates to a kind of The catalytic reforming system, the reforming system of particularly a kind of naphtha productive aromatic hydrocarbon and solvent oil.
Background technology
Along with rapid development of automobile industry and petrochemical industry to the aromatic hydrocarbons growth of requirement; particularly country is to the increasingly stringent requirement of environment protection, and catalytic reforming gasoline becomes one of ideal blend component in the New standard gasoline with its high-octane rating, low alkene and Trace Sulfur.For improving oil quality, the industry of development hydrogenation provides a large amount of cheap hydrogen sources to a large amount of hydrogen of catalytic reforming by product again.Therefore, catalytic reforming is being brought into play more and more important effect as the important oil refining process of producing stop bracket gasoline and aromatic hydrocarbons in oil refining, chemical engineering industry.
Catalytic reforming unit is pressed the catalyst regeneration mode, mainly can be divided into semi-regenerative reforming and CONTINUOUS REFORMER two classes at present.Two class catalytic reforming units are selected by its different raw material processing request by each refinery because of having different separately characteristics.
Semi-regenerative reforming is little owing to plant investment, flexible operation, and process cost is low, is suitable for different characteristics such as industrial scale, still takies critical role.
Since platinum/rhenium catalyst came out, the research of semi-regenerative reforming catalyzer and application had obtained sufficient development, have arrived quite high level.Half-regeneration reformer faces the pressure that enlarges processing power mostly, the capacity expansion revamping approach that yes deals with problems, but increase little device for load, if can be by improving catalyst activity, increasing the charging air speed, thereby improve unit capacity, then is best method.On the other hand, the reformer feed source presents diversified trend, and secondary processing oil such as the petroleum naphtha of low arene underwater content and coker gasoline proportion in reformer feed strengthens, and the poor quality trend of reformer feed is more and more obvious.The poor qualityization of raw material is had higher requirement to catalyst activity.
Therefore providing a kind of can improve processing power, and improves the naphtha productive aromatic hydrocarbon of liquid yield, aromatic production, octane value and hydrogen output and the difficult problem that all kinds of SOLVENTS reforming system just becomes this technical field urgent need solution thereof.
Summary of the invention
The purpose of this utility model provides and a kind ofly can improve processing power, and improves naphtha productive aromatic hydrocarbon and all kinds of SOLVENTS reforming system that liquid yield, aromatic production and hydrogen yield provide the high-octane rating product simultaneously.
For achieving the above object, the utility model is taked following technical scheme:
One of scheme:
A kind of naphtha productive aromatic hydrocarbon reforming system comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit is divided into two portions, first and/or second reaction unit by high-pressure separation apparatus, stabilizer tower system, extraction system be connected with water wash system and recovery system, described water wash system is connected with the system of raffinating oil, the described diced system of raffinating oil is connected with the 3rd and/or the 4th reaction unit again.
Two of scheme:
A kind of naphtha productive aromatic hydrocarbon reforming system comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit bottom is connected with high-pressure separator by pipeline; Described high-pressure separator is connected with the stabilizer tower system by pipeline on the one hand, is connected with reaction unit and another reaction unit by pipeline and compression set on the other hand; Described stabilizer tower system bottom is connected with extraction system by pipeline; Described extraction system bottom is connected with first recovery column by pipeline, described first recovery column top extraction benzene, and the bottom is connected with second recovery column by pipeline; Described second recovery column top extraction BTX aromatics, the bottom is connected with described extraction system by pipeline; Described extraction system top is connected with water wash system by pipeline; Described water wash system is connected with first Cutting Tap of raffinating oil by pipeline; The described first Cutting Tap top extraction food grade 6# solvent oil of raffinating oil; Described first Cutting Tap bottom of raffinating oil is connected with second Cutting Tap of raffinating oil by pipeline; The described second Cutting Tap top extraction technical grade 6# solvent oil of raffinating oil; Described second Cutting Tap bottom of raffinating oil is connected with the 3rd Cutting Tap of raffinating oil by pipeline; Described the 3rd Cutting Tap top extraction 120# solvent oil of raffinating oil; Described the 3rd Cutting Tap bottom of raffinating oil is connected with another reaction unit with heating unit by pipeline, the 200# of extraction simultaneously solvent oil; The other end of described another reaction unit is connected with described high-pressure separator by pipeline.
A kind of optimal technical scheme, it is characterized in that: described reaction unit is connected with second reaction unit (can link to each other with more reaction unit by heating unit behind second reaction unit) by second heating unit earlier again, and then is connected with described high-pressure separator.
A kind of optimal technical scheme, it is characterized in that: described another reaction unit is connected with the 4th reaction unit (can link to each other with more reaction unit by heating unit behind the 4th reaction unit) by the 4th heating unit again, and then is connected with described high-pressure separator.。
A kind of optimal technical scheme is characterized in that: described reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
A kind of optimal technical scheme is characterized in that: described another reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
The system of stabilizer tower described in the utility model and the diced system of raffinating oil comprise tower, air-cooler, watercooler, return tank, reflux pump and column bottoms pump etc. for conventional system.
Process furnace described in the utility model and condensing works are conventional device.
Catalyst system therefor described in the utility model in the reactor is conventional reforming catalyst.
Beneficial effect:
The advantage of naphtha productive aromatic hydrocarbon of the present utility model and all kinds of SOLVENTS reforming system thereof is: compare with existing The catalytic reforming system, in naphtha productive aromatic hydrocarbon of the present utility model and all kinds of SOLVENTS reforming system thereof, after the reacted product process extracting and the cutting of raffinating oil, the all kinds of SOLVENTS oil that generates with enter another reactor after recycle hydrogen mixes and further react, make the processing power of system of the present utility model improve, liquid yield, aromatic production and hydrogen yield improve greatly, and the product of high-octane rating and all kinds of SOLVENTS oil is provided simultaneously.
Below by the drawings and specific embodiments the utility model is described further, but and does not mean that restriction the utility model protection domain.
Description of drawings
Fig. 1 is the schematic flow sheet of the utility model embodiment 1.
Fig. 2 is the schematic flow sheet of the utility model embodiment 2.
Fig. 3 is the schematic flow sheet of the utility model embodiment 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment 1.With boiling range is 80-185 ℃, and sulphur content is 0.5ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 70% (m), and naphthene content is 28% (m), aromaticity content is 2% (m), and octane value (RON) is that 42,20 ℃ of density are 732 kilograms/meter
3, flow is the process heat exchange earlier of the refining feed naphtha (a) of 12.5 tons/hour paraffinic base, through after the process furnace 1-1 heating, enters reactor 2-1 and reacts again, the feed volume air speed is 3.0h
-1The temperature in of described reactor 2-1 is 530 ℃, and inlet pressure is 1.0MPa (A, an absolute pressure); The gained reaction product enters reactor 2-2 and reacts after heating through process furnace 1-2, and the temperature in of described reactor 2-2 is 530 ℃, and inlet pressure is 1.0MPa (A); Reaction product enters high-pressure separator 4 and carries out the high pressure separation after heat exchange and condenser 3 coolings, the service temperature of described high-pressure separator 4 is 35 ℃, and working pressure is 1.2MP*a (A); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.613 ton/hour, and hydrogen yield is 3.64% (weight); Other hydrogen is back to process furnace 1-1 and process furnace 1-3 through compressor 5, and wherein being back to the preceding hydrogen to oil volume ratio of process furnace 1-1 is 800: 1, and entering the preceding hydrogen to oil volume ratio of process furnace 1-3 is 1200: 1 (carrying out heat exchange before entering process furnace earlier); Handle through the stabilizer tower 6 that high-pressure separator 4 gained reformates enter in the stabilizer tower system, the tower top temperature of the stabilizer tower 6 in the described stabilizer tower system is 100 ℃, and pressure is 0.8MPa (A), and column bottom temperature is 220 ℃, pressure is 0.85MPa (A), and reflux ratio (m/m) is 0.90; Cat head extraction dry gas, liquefied gas and less water (c), its flow is 2.401 tons/hour; Gained reformed oil at the bottom of the tower (boiling range is 35-196 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 100 ℃, and working pressure is 0.6MPa (A), and solvent ratio is 3.0, returns and washes than being 0.5, and solvent for use is a tetramethylene sulfone; After extraction system 8 extractings, gained is extracted oil out and is entered first recovery column 9-1, and the tower top temperature of described first recovery column 9-1 is 85 ℃, and pressure is 0.1MPa (A), and column bottom temperature is 175 ℃, and pressure is 0.15MPa (A); Top extraction benzene (i), the purity of gained benzene are 99.99%, and freezing point is 5.45 ℃, and 20 ℃ of density are 879 kilograms/meter
3, flow is 0.274 ton/hour; The bottom production enters second recovery column 9-2, and the service temperature of described second recovery column is 110 ℃, and working pressure is 0.02MPa (A); Top extraction BTX aromatics (h), the gained BTX aromatics can be used as gasoline and is in harmonious proportion product or directly as aromatic hydrocarbon product, its boiling range is 80-196 ℃, sulphur content trace (can not detecting), non-aromatics content is 2.0% (m), aromaticity content is 98.0% (m), and octane value (RON) is that 129,20 ℃ of density are 861 kilograms/meter
3, flow is 8.780 tons/hour, aromatics yield is 71.03% (weight); After extraction system 8 extractings, gained is raffinated oil and is entered water wash system 10 through the top; Described water wash system 10 working pressures are 0.45MPa, and service temperature is 30 ℃, and water oil ratio is 0.1; Gained washing product enters the first Cutting Tap 7-1 that raffinates oil and cuts; The tower top temperature of the described first Cutting Tap 7-1 that raffinates oil is 86 ℃, and pressure is 0.16MPa, and column bottom temperature is 188 ℃, and pressure is 0.2MPa, and reflux ratio is 20; Described first Cutting Tap 7-1 top extraction food grade 6# solvent oil (d) boiling range of raffinating oil is 60-75 ℃, and aromaticity content is less than 0.1%, sulphur content trace (can not detecting), and 20 ℃ of density are 665 kilograms/meter
3, flow is 0.091 ton/hour; The described first Cutting Tap 7-1 bottom of raffinating oil is connected with the second Cutting Tap 7-2 that raffinates oil by pipeline; The tower top temperature of the described second Cutting Tap 7-2 that raffinates oil is 87 ℃, and pressure is 0.12MPa, and column bottom temperature is 191 ℃, and pressure is 0.16MPa, and reflux ratio is 20; Described second Cutting Tap 7-2 top extraction technical grade 6# solvent oil (e) boiling range of raffinating oil is 60-90 ℃, and aromaticity content is less than 1%, sulphur content trace (can not detecting), and 20 ℃ of density are 668 kilograms/meter
3, flow is 0.168 ton/hour; The described second Cutting Tap 7-2 bottom of raffinating oil is connected with the 3rd Cutting Tap 7-3 that raffinates oil by pipeline; The tower top temperature of described the 3rd Cutting Tap 7-3 that raffinates oil is 105 ℃, and pressure is 0.11MPa, and column bottom temperature is 214 ℃, and pressure is 0.15MPa, and reflux ratio is 20; Described the 3rd Cutting Tap 7-3 top extraction 120# solvent oil (f) boiling range of raffinating oil is 60-120 ℃, and aromaticity content is 710 kilograms/meter less than 3%, 20 ℃ of density
3, flow is 0.104 ton/hour; Described the 3rd Cutting Tap 7-3 bottom extraction treated oil (as the charging of reactor 2-3) of raffinating oil, a part is 140-200 ℃ a 200# solvent oil (g) as boiling range, and aromaticity content is lower than 15% (m), and 20 ℃ of density are 778 kilograms/meter
3, flow is 0.069 ton/hour, and total liquid recovery is 75.89%, and all the other treated oils react through entering reactor 2-3 after heating, and the temperature in of described reactor 2-3 is 530 ℃, inlet pressure is 1.0MPa (A); The gained reaction product enters reactor 2-4 reaction after process furnace 1-4 heating, the temperature in of described reactor 2-4 is 530 ℃, and inlet pressure is 1.0MPa (A), and the feed volume air speed is 1.0h
-1The gained reaction product with after the reaction product of described reactor 2-2 is mixed through entering high-pressure separator 4 after heat exchange and condenser 3 coolings.
Wherein pack into the ratio of catalytic amount of each reactor is reactor 2-1: reactor 2-2=1: 1.5; Reactor 2-3: reactor 2-4=1: 2.
The used reforming catalyst of the utility model is a kind of Pt, Re reforming catalyst, its carrier mixes by a certain percentage for single diaspore of GM and the single diaspore of Ziegler synthesising by-product SB that adopts aluminium colloidal sol deep fat ageing process and make, the compound γ-aluminium sesquioxide that two concentrated Kong Feng are arranged that makes through moulding, roasting.Pt content is 0.10～1.00 heavy % on the catalyzer, and Re content is 0.10～3.00 heavy %, and Cl content is 0.50～3.00 heavy %, and this catalyzer has the characteristics of high reactivity, highly selective and low carbon deposit.
Total liquid yield equals the flow sum of benzene, BTX aromatics, food grade 6# solvent oil, technical grade 6# solvent oil, 120# solvent oil and 200# solvent oil divided by the raw material inlet amount in the utility model.
Aromatics yield equals benzene and BTX aromatics flow sum multiply by aromaticity content again divided by the raw material inlet amount.
Hydrogen yield equals to efflux the hydrogen amount and multiply by hydrogen purity again divided by the raw material inlet amount.
The physico-chemical property of reactor 2-1 and 2-2 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 192 | 183 | 0.52 | 0.75 | 0.25 | 0.25 |
The physico-chemical property of reactor 2-3 and 2-4 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 196 | 187 | 0.54 | 0.74 | 0.26 | 0.45 |
The used measuring method of the utility model is (down together):
1, boiling range: GB/T6536-1997 measured for petroleum product distillation method;
2, sulphur content: the total sulfur content assay method (ultraviolet fluorescence method) of SH/T0689-2000 light hydrocarbon and motor spirit and other oil products;
3, mercaptan sulfur: mercaptan sulfur assay method (potentiometric titration) in the GB/T1792-1988 distillate fuel oil;
4, alkane: SH/T0239-92 thin layer packed column chromatography;
5, aromatic hydrocarbons: GB/T11132-2002 liquid petroleum product hydro carbons assay method (fluorescent indicator adsorption method);
6, octane value: GB/T5487 testing octane number of gasoline method (organon);
7, density: GB/T1884-2000 crude oil and liquid petroleum product density experiment chamber assay method (densimeter method);
8, naphthenic hydrocarbon: SH/T0239-92 thin layer packed column chromatography;
9, metal in the oil: the standard test methods of nickel, vanadium and iron in ASTM D 5708-2005 inductively coupled plasma (ICP) aes determination crude oil and the trapped fuel;
10, nitrogen content: the SH/T0704-2001 chemoluminescence method is surveyed nitrogen (boat sample introduction).
Embodiment 2
As shown in Figure 2, be the schematic flow sheet of the utility model embodiment 2.With boiling range is 80-185 ℃, and sulphur content is 0.54ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 60% (m), and naphthene content is 34% (m), aromaticity content is 6% (m), and octane value (RON) is that 50,20 ℃ of density are 738 kilograms/meter
3, flow is the process heat exchange earlier of the refining feed naphtha (a) of 12.5 tons/hour intermediate base, through after the process furnace 1-1 heating, enters reactor 2-1 and reacts again; The feed volume air speed is 4.0h
-1, described reactor 2-1 goes up for reactor 2-1 and following two reactors in series of reactor 2-1 are formed, and is provided with process furnace 1-2 between two reactors; The temperature in of described reactor 2-1 is 500 ℃, and inlet pressure is 1.3MPa (A); Enter high-pressure separator 4 through reactor 2-1 reaction back products therefrom after heat exchange and condenser 3 coolings and carry out the high pressure separation, the service temperature of described high-pressure separator 4 is 40 ℃, and working pressure is 1.3MPa (A); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.474 ton/hour, and hydrogen yield is 3.42% (weight); After other hydrogen was back to process furnace 1-1 and well heater 1-3 through compressor 5, the hydrogen to oil volume ratio that wherein is back to behind the process furnace 1-1 was 800: 1, and the hydrogen to oil volume ratio that enters behind the process furnace 1-3 is 1200: 1 (carrying out heat exchange before entering reaction unit earlier); Handle through the stabilizer tower 6 that high-pressure separator 4 gained reformates enter in the stabilizer tower system, the tower top temperature of the stabilizer tower 6 in the described stabilizer tower system is 102 ℃, and pressure is 0.95MPa (A), and column bottom temperature is 227.5 ℃, pressure is 1.0MPa (A), and reflux ratio (m/m) is 0.99; Cat head extraction dry gas, liquefied gas and less water (c), its flow is 1.448 tons/hour; Gained reformed oil at the bottom of the tower (boiling range is 35-194 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 120 ℃, and working pressure is 0.8MPa (A), and solvent ratio is 5, returns and washes than being 0.7, and solvent for use is the N-formyl morpholine; After extraction system 8 extractings, gained is extracted oil out and is entered first recovery column 9-1, and the tower top temperature of described first recovery column is 87 ℃, and pressure is 0.15MPa (A), and column bottom temperature is 175 ℃, and pressure is 0.2MPa (A); Top extraction benzene (i), the purity of gained benzene are 99.99%, and freezing point is 5.45 ℃, and 20 ℃ of density are 879 kilograms/meter
3, flow is 0.454 ton/hour; The bottom production enters second recovery column 9-2, and the service temperature of described second recovery column is 130 ℃, and working pressure is 0.035MPa (A); Top extraction BTX aromatics (h), the gained BTX aromatics can be used as gasoline and is in harmonious proportion product or directly as aromatic hydrocarbon product, its boiling range is 80-194 ℃, sulphur content trace (can not detecting), non-aromatics content is 1.9% (m), aromaticity content is 98.1% (m), and octane value (RON) is that 131,20 ℃ of density are 862 kilograms/meter
3, flow is 9.650 tons/hour, aromatics yield is 79.37% (weight); The bottom production returns and enters extraction system 8; Through after extraction system 8 extractings, gained is raffinated oil and is entered water wash system 10 through the top and handle; The working pressure of described water wash system 10 is 0.5MPa, and service temperature is 40 ℃, and water oil ratio is 0.3; After water wash system 10 washings, products obtained therefrom enters the first Cutting Tap 7-1 that raffinates oil and cuts; The tower top temperature of the described first Cutting Tap 7-1 that raffinates oil is 96 ℃, and pressure is 0.20MPa, and column bottom temperature is 198 ℃, and pressure is 0.24MPa, and reflux ratio is 40; Described first Cutting Tap 7-1 top extraction food grade 6# solvent oil (d) boiling range of raffinating oil is 60-75 ℃, and aromaticity content is less than 0.1%, sulphur content trace (can not detecting), and 20 ℃ of density are 665 kilograms/meter
3, flow is 0.109 ton/hour; The described first Cutting Tap 7-1 bottom of raffinating oil is connected with the second Cutting Tap 7-2 that raffinates oil by pipeline; The tower top temperature of the described second Cutting Tap 7-2 that raffinates oil is 97 ℃, and pressure is 0.14MPa, and column bottom temperature is 201 ℃, and pressure is 0.2MPa, and reflux ratio is 40; Described second Cutting Tap 7-2 top extraction technical grade 6# solvent oil (e) boiling range of raffinating oil is 60-90 ℃, and aromaticity content is less than 1%, sulphur content trace (can not detecting), and 20 ℃ of density are 670 kilograms/meter
3, flow is 0.180 ton/hour; The described second Cutting Tap 7-2 bottom of raffinating oil is connected with the 3rd Cutting Tap 7-3 that raffinates oil by pipeline; The tower top temperature of described the 3rd Cutting Tap 7-3 that raffinates oil is 115 ℃, and pressure is 0.15MPa, and column bottom temperature is 224 ℃, and pressure is 0.19MPa, and reflux ratio is 40; Described the 3rd Cutting Tap 7-3 top extraction 120# solvent oil (f) boiling range of raffinating oil is 60-120 ℃, and aromaticity content is 712 kilograms/meter less than 3%, 20 ℃ of density
3, flow is 0.123 ton/hour; Described the 3rd Cutting Tap 7-3 bottom extraction treated oil (as the charging of reactor 2-3) of raffinating oil, a part is 140-200 ℃ a 200# solvent oil (g) as boiling range, and aromaticity content is lower than 15% (m), and 20 ℃ of density are 779 kilograms/meter
3, flow is 0.062 ton/hour, total liquid recovery is 84.62%; Enter reactor 2-2 after all the other gained treated oils heat through process furnace 1-3 and react, the temperature in of described reactor 2-2 is 500 ℃, and inlet pressure is 1.3MPa (A), and the feed volume air speed is 1.5h
-1Described reactor 2-2 is gone up by reactor 2-2 and following two reactors in series of reactor 2-2 are formed, between be provided with process furnace 1-4; Wherein pack into the ratio of catalytic amount of each reactor is on the reactor 2-2: under the reactor 2-2=1: 2.5; Enter high-pressure separator 4 after process heat exchange of gained reaction product and condenser 3 coolings.
Pack into the ratio of catalytic amount of each reactor is on the reactor 2-1: under the reactor 2-1=1: 2.
The physico-chemical property of reactor 2-1 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 192 | 183 | 0.52 | 0.75 | 0.25 | 0.25 |
The physico-chemical property of reactor 2-2 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 196 | 187 | 0.54 | 0.74 | 0.26 | 0.45 |
Embodiment 3
As shown in Figure 3, be the schematic flow sheet of the utility model embodiment 3.With boiling range is 80-185 ℃, and sulphur content is 0.45ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 47% (m), and naphthene content is 42% (m), aromaticity content is 11% (m), and octane value (RON) is that 61,20 ℃ of density are 742 kilograms/meter
3, flow is the process heat exchange earlier of the refining petroleum naphtha (a) of 12.5 tons/hour cycloalkyl, through after the process furnace 1-1 heating, enters reactor 2-1 and reacts again; The feed volume air speed is 5.0h
-1The temperature in of described reactor 2-1 is 470 ℃, and inlet pressure is 1.6MPa (A); The gained reaction product enters high-pressure separator 4 and carries out the high pressure separation after heat exchange and condenser 3 coolings, the service temperature of described high-pressure separator 4 is 45 ℃, and working pressure is 1.4MPa (A); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.419 ton/hour, and pure hydrogen flow is 0.382 ton/hour, and hydrogen yield is 3.06% (weight); Other hydrogen is back to process furnace 1-1 and process furnace 1-2 through compressor 5, and wherein being back to the preceding hydrogen to oil volume ratio of process furnace 1-1 is 800: 1, and entering the preceding hydrogen to oil volume ratio of process furnace 1-2 is 1200: 1 (carrying out heat exchange before entering process furnace earlier); Enter stabilizer tower system 6 through high-pressure separator 4 gained reformates and handle, the tower top temperature of described stabilizer tower system 6 is 120 ℃, and pressure is 1.05MPa (A), and column bottom temperature is 240 ℃, and pressure is 1.10MPa (A), and reflux ratio (m/m) is 1.15; Cat head extraction dry gas, liquefied gas and less water (c), its flow is 1.565 tons/hour; Gained reformed oil at the bottom of the tower (boiling range is 35-192 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 150 ℃, and working pressure is 1.0MPa (A), and solvent ratio is 8.0, returns and washes than being 1.0, and solvent for use is a Tetraglycol 99; After extraction system 8 extractings, gained is extracted oil out and is entered first recovery column 9-1, and the tower top temperature of described first recovery column is 90 ℃, and pressure is 0.2MPa (A), and column bottom temperature is 175 ℃, and pressure is 0.25MPa (A); Top extraction benzene (f), the purity of gained benzene are 99.99%, and freezing point is 5.45 ℃, and 20 ℃ of density are 879 kilograms/meter
3, flow is 0.335 ton/hour; The bottom production enters second recovery column 9-2, and the service temperature of described second recovery column is 155 ℃, and working pressure is 0.05MPa (A); Top extraction BTX aromatics (e), the gained BTX aromatics can be used as gasoline and is in harmonious proportion product or directly as aromatic hydrocarbon product, its boiling range is 80-192 ℃, sulphur content trace (can not detecting), non-aromatics content is 1.8% (m), aromaticity content is 98.2% (m), and octane value (RON) is that 134,20 ℃ of density are 865 kilograms/meter
3, flow is 9.903 tons/hour, aromatics yield is 80.48% (weight); The bottom production returns and enters extraction system 8; Through after extraction system 8 extractings, gained is raffinated oil and is entered water wash system 10 through the top and handle; Described water wash system 10 working pressures are 0.55MPa, and service temperature is 50 ℃, and water oil ratio is 0.5; After the water wash system washing, products obtained therefrom enters the first Cutting Tap 7-1 that raffinates oil and cuts; The tower top temperature of the described first Cutting Tap 7-1 that raffinates oil is 106 ℃, and pressure is 0.24MPa, and column bottom temperature is 208 ℃, and pressure is 0.28MPa, and reflux ratio is 60; Described first Cutting Tap 7-1 top extraction food grade 6# solvent oil (d) boiling range of raffinating oil is 60-75 ℃, and aromaticity content is less than 0.1%, sulphur content trace (can not detecting), and 20 ℃ of density are 666 kilograms/meter
3, flow is 0.067 ton/hour; The described first Cutting Tap 7-1 bottom of raffinating oil is connected with the second Cutting Tap 7-2 that raffinates oil by pipeline; The tower top temperature of the described second Cutting Tap 7-2 that raffinates oil is 107 ℃, and pressure is 0.20MPa, and column bottom temperature is 211 ℃, and pressure is 0.24MPa, and reflux ratio is 60; Described second Cutting Tap 7-2 top extraction technical grade 6# solvent oil (e) boiling range of raffinating oil is 60-90 ℃, and aromaticity content is less than 1%, sulphur content trace (can not detecting), and 20 ℃ of density are 671 kilograms/meter
3, flow is 0.106 ton/hour; The described second Cutting Tap 7-2 bottom of raffinating oil is connected with the 3rd Cutting Tap 7-3 that raffinates oil by pipeline; The tower top temperature of described the 3rd Cutting Tap 7-3 that raffinates oil is 125 ℃, and pressure is 0.19MPa, and column bottom temperature is 234 ℃, and pressure is 0.23MPa, and reflux ratio is 60; Described the 3rd Cutting Tap 7-3 top extraction 120# solvent oil (f) boiling range of raffinating oil is 60-120 ℃, and aromaticity content is 714 kilograms/meter less than 3%, 20 ℃ of density
3, flow is 0.072 ton/hour; Described the 3rd Cutting Tap 7-3 bottom extraction treated oil (as the charging of reactor 2-3) of raffinating oil, a part is 140-200 ℃ a 200# solvent oil (g) as boiling range, and aromaticity content is lower than 15% (m), and 20 ℃ of density are 780 kilograms/meter
3, flow is 0.033 ton/hour, total liquid recovery is 84.13%; Enter reactor 2-2 after described all the other treated oils heat through process furnace 1-2 and react, the temperature in of described reactor 2-2 is 470 ℃, and inlet pressure is 1.6MPa (A), and the feed volume air speed is 2.0h
-1Enter high-pressure separator 4 after process heat exchange of gained reaction product and condenser 3 coolings.
Pack into the ratio of catalytic amount of each reactor is reactor 2-1: reactor 2-2=1: 2;
The physico-chemical property of reactor 2-1 catalyst system therefor is as shown in the table:
| Specific surface area | Intensity N/cm | Pore volume ml/g | Bulk density | Pt | Re |
| m 2/g | g/ml | m％ | m％ | ||
| 192 | 183 | 0.52 | 0.75 | 0.25 | 0.25 |
The physico-chemical property of reactor 2-2 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％ | Re m％ |
| 196 | 187 | 0.54 | 0.74 | 0.26 | 0.45 |
Claims (6)
1. a naphtha productive aromatic hydrocarbon reforming system comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit is divided into two portions, first and/or second reaction unit is connected with the diced system of raffinating oil by high-pressure separation apparatus, stabilizer tower system, extraction system, recovery system, water wash system, and the described diced system of raffinating oil is connected with the 3rd and/or the 4th reaction unit simultaneously.
2. a naphtha productive aromatic hydrocarbon reforming system comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit bottom is connected with high-pressure separator by pipeline; Described high-pressure separator is connected with the stabilizer tower system by pipeline on the one hand, is connected with reaction unit and another reaction unit by pipeline and compression set on the other hand; Described stabilizer tower system bottom is connected with extraction system by pipeline; Described extraction system bottom is connected with first recovery column by pipeline, described first recovery column top extraction benzene, and the bottom is connected with second recovery column by pipeline; Described second recovery column top extraction BTX aromatics, the bottom is connected with described extraction system by pipeline; Described extraction system top is connected with water wash system by pipeline; Described water wash system is connected with first Cutting Tap of raffinating oil by pipeline; The described first Cutting Tap top extraction food grade 6# solvent oil of raffinating oil; Described first Cutting Tap bottom of raffinating oil is connected with second Cutting Tap of raffinating oil by pipeline; The described second Cutting Tap top extraction technical grade 6# solvent oil of raffinating oil; Described second Cutting Tap bottom of raffinating oil is connected with the 3rd Cutting Tap of raffinating oil by pipeline; Described the 3rd Cutting Tap top extraction 120# solvent oil of raffinating oil; Described the 3rd Cutting Tap bottom of raffinating oil is connected with another reaction unit with heating unit by pipeline, the 200# of extraction simultaneously solvent oil; The other end of described another reaction unit is connected with described high-pressure separator by pipeline.
3. naphtha productive aromatic hydrocarbon reforming system according to claim 2 is characterized in that: described reaction unit is connected with second reaction unit by second heating unit, and then is connected with described high-pressure separator.
4. naphtha productive aromatic hydrocarbon reforming system according to claim 3 is characterized in that: described another reaction unit is connected with the 4th reaction unit by the 4th heating unit, and then is connected with described high-pressure separator.
5. according to claim 3 or 4 described naphtha productive aromatic hydrocarbon reforming systems, it is characterized in that: described reaction unit is two reactors in series up and down, is connected by heating unit therebetween.
6. naphtha productive aromatic hydrocarbon reforming system according to claim 5 is characterized in that: described another reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
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| CN2009202783763U CN201620141U (en) | 2009-12-22 | 2009-12-22 | Reforming system for fecundation of aromatic hydrocarbon and solvent oil with naphtha |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105219422A (en) * | 2015-10-30 | 2016-01-06 | 西北大学 | A kind ofly be applicable to the composite extractant of coal-based petroleum naphtha and prepare the method for solvent oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105219422A (en) * | 2015-10-30 | 2016-01-06 | 西北大学 | A kind ofly be applicable to the composite extractant of coal-based petroleum naphtha and prepare the method for solvent oil |
| CN105219422B (en) * | 2015-10-30 | 2017-05-03 | 西北大学 | Composite extracting agent suitable for coal-based naphtha and method for preparing solvent naphtha |
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