CN201459048U - Reforming system for fecundating aromatics extracted by evaporation dehydration system with side stream - Google Patents
Reforming system for fecundating aromatics extracted by evaporation dehydration system with side stream Download PDFInfo
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- CN201459048U CN201459048U CN200920109184XU CN200920109184U CN201459048U CN 201459048 U CN201459048 U CN 201459048U CN 200920109184X U CN200920109184X U CN 200920109184XU CN 200920109184 U CN200920109184 U CN 200920109184U CN 201459048 U CN201459048 U CN 201459048U
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Abstract
The utility model discloses a reforming system for fecundating aromatics by adopting naphtha and a method. The system comprises a heating device and reaction devices. The utility model is characterized in that the reaction device is connected with a high pressure separator and the high pressure separator is connected with a stabilization tower system; the lower part of the stabilization tower system is connected with an extraction system by a pipeline; on the one hand, the extraction system is connected with an evaporation dehydration system by a pipeline and on the other hand extracts mixed aromatics through pipelines; water is directly extracted from the top of the evaporation dehydration system through pipelines, light raffinate oil is extracted from the side of the evaporation dehydration system through pipelines and the bottom of the evaporation dehydration system is connected with the other reaction device by a pipeline and the heating device; and the other end of the other reaction device is connected with the high pressure separator by a pipeline. The reforming system of the utility model has the following advantage: the handling capacity, the liquid yield, the aromatics productivity and the hydrogen output are greatly increased.
Description
Technical field
The utility model relates to a kind of reforming system, the reforming system for productive aromatic hydrocarbon of particularly a kind of evaporation and dehydration system tape side line extraction.
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 the naphtha productive aromatic hydrocarbon reforming system of raising liquid yield, aromatic production, octane value and hydrogen output just becomes the difficult problem that this technical field is badly in need of solution.
Summary of the invention
The purpose of this utility model provides and a kind ofly can improve processing power, and improves the naphtha productive aromatic hydrocarbon 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:
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 (and/or more reaction units) is connected with evaporation and dehydration system by high-pressure separator, stabilizer tower system and extraction system, and described evaporation and dehydration system is connected with the 3rd and/or the 4th reaction unit (and/or more reaction units) again; Described evaporation and dehydration system tape has side line extraction mouth.
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, and is connected with the raw material supply system by pipeline and compression set; Described stabilizer tower system bottom is connected with extraction system by pipeline; Described extraction system is connected with evaporation and dehydration system by pipeline on the one hand; Described extraction system is on the other hand by pipeline extraction BTX aromatics; Described evaporation and dehydration system top is by the pipeline recovered water, described evaporation and dehydration system sidepiece is raffinated oil by pipeline extraction lightweight, described evaporation and dehydration system bottom is connected with another reaction unit (the 3rd reaction unit) by pipeline and heating unit, and the other end of described another reaction unit is connected with described high-pressure separator with refrigerating unit 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 again by heating unit behind the 4th reaction unit) by the 4th heating unit earlier, 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.
Extraction system described in the utility model is that the patent No. is a disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation, water wash system, returns the system of washing etc.
System of stabilizer tower described in the utility model and evaporation and dehydration system are conventional system, comprise tower, air-cooler, watercooler, return tank, reflux pump and column bottoms pump etc.
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 reforming system of the present utility model is: compare with existing catalytic reforming process, in naphtha productive aromatic hydrocarbon reforming system of the present utility model and the method, under than low reaction pressure reacted product through extracting and dehydration by evaporation after, the treated 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 high-octane rating product 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 (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 (absolute pressure); 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 1.2MPa (absolute pressure); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.588 ton/hour, and pure hydrogen flow is 0.436 ton/hour, and hydrogen yield is 3.49% (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); Entering stabilizer tower system 6 through high-pressure separator 4 gained reformates handles, the tower top temperature of described stabilizer tower system 6 is 100 ℃, and pressure is 0.8MPa (absolute pressure), and column bottom temperature is 220 ℃, pressure is 0.85MPa (absolute pressure), and reflux ratio (m/m) is 0.90; Cat head extraction dry gas, liquefied gas and less water (c), its flow is 2.260 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 (absolute pressure), and solvent ratio is 3.0, returns and washes than being 0.5, and solvent for use is a tetramethylene sulfone; Through after the extracting, gained BTX aromatics (e) extraction is as gasoline mediation product or directly as aromatic hydrocarbon product, the boiling range of gained BTX aromatics is 75-196 ℃, 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 9.117 tons/hour, aromatics yield is 71.48% (weight); Through after the extracting, the gained dehydration by evaporation tower 7 (other does not draw) that top through extraction system 8 enters in the evaporation and dehydration system of raffinating oil dewaters, the head temperature of the dehydration by evaporation tower 7 in the described evaporation and dehydration system is 110 ℃, pressure is 0.4MPa (absolute pressure), bottom temp is 210 ℃, pressure is 0.45MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; Dehydration by evaporation tower 7 in the described evaporation and dehydration system is provided with side line extraction mouth, its temperature is 128 ℃, pressure is 0.41MPa (absolute pressure), the extraction lightweight is raffinated oil (f), and the boiling range that described lightweight is raffinated oil is 35-75 ℃, sulphur content trace (can not detecting), non-aromatics content is 99.9% (m), aromaticity content is 0.1% (m), and octane value (RON) is that 69,20 ℃ of density are 564 kilograms/meter
3, flow is 0.534 ton/hour, it not only can be used as gasoline mediation product but also can be used as the cracking of ethylene raw material; Total liquid yield is 77.21%; Dehydration by evaporation tower 7 bottom extraction treated oils in the described evaporation and dehydration system are as the charging of reactor 2-3, the boiling range of gained treated oil is 35-186 ℃, sulphur content trace (can not detecting), non-aromatics content is 98.8% (m), aromaticity content is 1.2% (m), octane value (RON) is that 63,20 ℃ of density are 738 kilograms/meter
3, flow is 4.292 tons/hour; Enter reactor 2-3 after the gained treated oil heats through process furnace 1-3 and react, the temperature in of described reactor 2-3 is 530 ℃, and inlet pressure is 1.0MPa (absolute pressure); 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 (absolute pressure), 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 flow sum that BTX aromatics, lightweight raffinate oil divided by the raw material inlet amount in the utility model.
Aromatics yield equals the BTX aromatics flow and 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
-1Wherein said reactor 2-1 is gone up by reactor 2-1 and following two reactors in series of reactor 2-1 are formed, on the described reactor 2-1 and the temperature under the reactor 2-1 be 500 ℃, inlet pressure is 1.3MPa (absolute pressure); Be connected by process furnace 1-2 between two reactors; 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 (absolute pressure); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.439 ton/hour, and pure hydrogen flow is 0.396 ton/hour, and hydrogen yield is 3.17% (weight); Other hydrogen is back to process furnace 1-1 and well heater 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 reaction unit earlier); Entering stabilizer tower system 6 through high-pressure separator 4 gained reformates handles, the tower top temperature of described stabilizer tower system 6 is 102 ℃, and pressure is 0.95MPa (absolute pressure), and column bottom temperature is 227.5 ℃, pressure is 1.00MPa (absolute pressure), and reflux ratio (m/m) is 0.99; Cat head extraction dry gas, liquefied gas and less water (c), its flow is 1.198 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 (absolute pressure), and solvent ratio is 5, returns and washes than being 0.7, and solvent for use is the N-formyl morpholine; Through after the extracting, gained BTX aromatics (e) extraction is as gasoline mediation product or directly as aromatic hydrocarbon product, the boiling range of gained BTX aromatics is 75-194 ℃, 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 9.445 tons/hour, aromatics yield is 74.12% (weight); Through after the extracting, the gained dehydration by evaporation tower 7 (other does not draw) that top through extraction system 8 enters in the evaporation and dehydration system of raffinating oil dewaters, the head temperature of the dehydration by evaporation tower 7 in the described evaporation and dehydration system is 120 ℃, pressure is 0.5MPa (absolute pressure), bottom temp is 225 ℃, pressure is 0.55MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; The side line of the dehydration by evaporation tower 7 in the described evaporation and dehydration system is provided with the extraction mouth, the temperature of this extraction mouth is 141 ℃, pressure is 0.51MPa (absolute pressure), the extraction lightweight is raffinated oil (f), and the boiling range that described lightweight is raffinated oil is 35-75 ℃, sulphur content trace (can not detecting), non-aromatics content is 99.8% (m), aromaticity content is 0.2% (m), and octane value (RON) is that 70,20 ℃ of density are 571 kilograms/meter
3, flow is 1.418 tons/hour, it not only can be used as gasoline mediation product but also can be used as the cracking of ethylene raw material; Total liquid yield is 86.91%; Described evaporation and dehydration system bottom extraction treated oil (as the charging of the second reactor 2-2), the boiling range of gained treated oil is 35-184 ℃, sulphur content trace (can not detecting), non-aromatics content is 98.7% (m), aromaticity content is 1.3% (m), octane value (RON) is that 63,20 ℃ of density are 740 kilograms/meter
3, flow is 4.492 tons/hour; The gained treated oil enters reactor 2-2 after through process furnace 1-3 heating and reacts, and described reactor 2-2 is gone up by reactor 2-2 and following two reactors in series of reactor 2-2 are formed, between pass through process furnace 1-4 connection; Described reactor 2-2 go up and reactor 2-2 under temperature in be 500 ℃, inlet pressure is 1.3MPa (absolute pressure), the feed volume air speed is 1.5h
-1Enter high-pressure separator 4 after process heat exchange of gained reaction product and condenser 3 coolings.
Wherein pack into the ratio of catalytic amount of each reactor is on the reactor 2-1: under the reactor 2-1=1: 2; On the reactor 2-2: under the reactor 2-2=1: 2.5.
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 (absolute pressure); 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 (absolute pressure); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.366 ton/hour, and pure hydrogen flow is 0.336 ton/hour, and hydrogen yield is 2.69% (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); Entering stabilizer tower system 6 through high-pressure separator 4 gained reformates handles, the tower top temperature of described stabilizer tower system 6 is 120 ℃, and pressure is 1.05MPa (absolute pressure), and column bottom temperature is 240 ℃, pressure is 1.10MPa (absolute pressure), and reflux ratio (m/m) is 1.15; Cat head extraction dry gas, liquefied gas and less water (c), its flow is 0.670 ton/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 (absolute pressure), and solvent ratio is 8.0, returns and washes than being 1.0, and solvent for use is a Tetraglycol 99; Through after the extracting, gained BTX aromatics (e) extraction is as gasoline mediation product or directly as aromatic hydrocarbon product, the boiling range of gained BTX aromatics is 75-192 ℃, 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 9.311 tons/hour, aromatics yield is 73.15% (weight); Through after the extracting, the gained dehydration by evaporation tower 7 (other does not draw) that top through extraction system 8 enters in the evaporation and dehydration system of raffinating oil dewaters, the head temperature of the dehydration by evaporation tower 7 in the described evaporation and dehydration system is 130 ℃, pressure is 0.6MPa (absolute pressure), bottom temp is 240 ℃, pressure is 0.65MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; Described evaporation and dehydration system side line extraction mouth temperature is 153 ℃, pressure is 0.61MPa (absolute pressure), extraction lightweight raffinate oil (f), the boiling range that described lightweight is raffinated oil is 35-75 ℃, sulphur content trace (can not detecting), non-aromatics content are 99.7% (m), and aromaticity content is 0.3% (m), octane value (RON) is that 71,20 ℃ of density are 575 kilograms/meter
3, flow is 2.153 tons/hour, it not only can be used as gasoline mediation product but also can be used as the cracking of ethylene raw material; Total liquid yield is 91.71%; Described evaporation and dehydration system bottom extraction treated oil (as the charging of reactor 2-2), the boiling range of gained treated oil is 35-182 ℃, sulphur content trace (can not detecting), non-aromatics content is 1.5% (m), aromaticity content is 98.5% (m), octane value (RON) is 64, is 745 kilograms/meter 20 ℃ of density
3, flow is 3.959 tons/hour; Enter reactor 2-2 after described treated oil heats through process furnace 1-2 and react, the temperature in of described reactor 2-2 is 470 ℃, and inlet pressure is 1.6MPa (absolute pressure), 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.
Wherein 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 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 |
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 evaporation and dehydration system by high-pressure separator, stabilizer tower system and extraction system, and described evaporation and dehydration system is connected with the 3rd and/or the 4th reaction unit again; Described evaporation and dehydration system tape has side line extraction mouth.
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, and is connected with the raw material supply system by pipeline and compression set; Described stabilizer tower system bottom is connected with extraction system by pipeline; Described extraction system is connected with evaporation and dehydration system by pipeline on the one hand; Described extraction system is on the other hand by pipeline extraction BTX aromatics; Described evaporation and dehydration system top is by the pipeline recovered water, described evaporation and dehydration system sidepiece is raffinated oil by pipeline extraction lightweight, described evaporation and dehydration system bottom is connected with another reaction unit by pipeline and heating unit, and the other end of described another reaction unit is connected with described high-pressure separator with refrigerating unit 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 earlier, 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 earlier, and then is connected with described high-pressure separator.
5. naphtha productive aromatic hydrocarbon reforming system according to claim 2 is characterized in that: described reaction unit is placed in-line two reactors 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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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200920109184XU CN201459048U (en) | 2009-06-17 | 2009-06-17 | Reforming system for fecundating aromatics extracted by evaporation dehydration system with side stream |
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| CN200920109184XU CN201459048U (en) | 2009-06-17 | 2009-06-17 | Reforming system for fecundating aromatics extracted by evaporation dehydration system with side stream |
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| CN201459048U true CN201459048U (en) | 2010-05-12 |
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