CN201459036U - Naphtha reforming system for producing raffinate oil, benzene and mixed aromatics - Google Patents
Naphtha reforming system for producing raffinate oil, benzene and mixed aromatics Download PDFInfo
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- CN201459036U CN201459036U CN2009201091869U CN200920109186U CN201459036U CN 201459036 U CN201459036 U CN 201459036U CN 2009201091869 U CN2009201091869 U CN 2009201091869U CN 200920109186 U CN200920109186 U CN 200920109186U CN 201459036 U CN201459036 U CN 201459036U
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Abstract
The utility model discloses a reforming system for increasing the yield of aromatics with naphtha. The system comprises a heating device and a reaction device, and is characterized in that the reaction device is connected with a high pressure separator; 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 through a pipeline; the stabilization tower system is provided with a side-stream extraction opening; one the one hand, the extraction system is connected with an evaporation and dehydration system through a pipeline, and on the other hand, the extraction system is connected with a first reclaiming tower through a pipeline; benzene is extracted from the upper part of the first reclaiming tower through a pipeline, and the lower part of the first reclaiming tower is connected with a second reclaiming tower through a pipeline; mixed aromatics is extracted from the upper part of the second reclaiming tower through a pipeline, and the lower part of the second reclaiming tower is connected with the extraction system through a pipeline; one the one hand, the bottom of the evaporation and dehydration system is connected with another reaction device through a pipeline and the heating device, and on the other hand, raffinate oil is extracted from the lower part of the evaporation and dehydration system through a pipeline; water is directly extracted from the top part of the evaporation and dehydration system through a pipeline; and the other end of another reaction device is connected with the high pressure separator through a pipeline. The reforming system for increasing the yield of the aromatics with the naphtha provided by the utility model has the advantage of greatly increasing processing capability, liquid yield, aromatics yield and hydrogen output.
Description
Technical field
The utility model relates to a kind of reforming system, and particularly a kind of production is raffinated oil, the naphtha reforming system of benzene and BTX aromatics.
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 is connected with evaporation and dehydration system by high-pressure separator, stabilizer tower system and extraction system, described extraction system links to each other with first and second recovery towers again, described evaporation and dehydration system is connected with the 3rd and/or the 4th reaction unit again, and described stabilizer tower system is provided with 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, and described stabilizer tower system is provided with side line extraction mouth; Described extraction system is connected with evaporation and dehydration system by pipeline on the one hand; Described extraction system is connected with first recovery column by pipeline on the other hand; Described first recovery column top is by pipeline extraction benzene, and the bottom is connected with second recovery column by pipeline; Described second recovery column top is by pipeline extraction BTX aromatics, and the bottom is connected with extraction system by pipeline; Described evaporation and dehydration system top is by the pipeline recovered water, described evaporation and dehydration system bottom is connected with another reaction unit (the 3rd reaction unit) by pipeline and heating unit on the one hand, raffinates oil by the pipeline extraction on the other hand in described evaporation and dehydration system bottom; 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, the high-octane rating product is provided simultaneously, owing to isolated benzene, make the benzene content of premium blend component BTX aromatics reduce greatly in addition.
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, schematic flow sheet for the utility model embodiment 1. with boiling range is 80-185 ℃, sulphur content is 0.5ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content is 70% (m), and naphthene content is 28% (m), and aromaticity content is 2% (m), 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 0.522 ton/hour, and pure hydrogen flow is 0.389 ton/hour, and hydrogen yield is 3.11% (weight); Other hydrogen is back to feed line 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 1.923 tons/hour; Described stabilizer tower system 6 side line extraction mouth temperature are 128 ℃, and pressure is 0.81MPa (absolute pressure), extraction petroleum naphtha (g); The boiling range of described petroleum naphtha is 35-75 ℃, and sulphur content trace (can not detecting), non-aromatics content are 99.9% (m), and aromaticity content is 0.1% (m), and octane value (RON) is that 69,20 ℃ of density are 564 kilograms/meter
3, flow is 0.979 ton/hour, it not only can be used as gasoline mediation product but also can be used as the cracking of ethylene raw material; Gained reformed oil (boiling range is 75-196 ℃) enters extraction system 8 and handles at the bottom of described stabilizer tower system 6 towers, the service temperature of described extraction system 8 is 100 ℃, and working pressure is 0.6MPa (absolute pressure), and solvent ratio is 3.0, return and wash than being 0.5, 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 is 85 ℃, and pressure is 0.1MPa (absolute pressure), and column bottom temperature is 175 ℃, and pressure is 0.15MPa (absolute pressure); Top extraction benzene (h), 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 0.210 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 (absolute pressure); 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 80-196 ℃, sulphur content trace (can not detecting), non-aromatics content is 2.0% (m), and aromaticity content is 98.0% (m), and benzene content is 0.29% (m), octane value (RON) is that 129,20 ℃ of density are 861 kilograms/meter
3, flow is 7.926 tons/hour, aromatics yield is 63.82% (weight); The bottom production returns and enters extraction system; Through after extraction system 8 extractings, raffinate oil top through extraction system 8 of gained enters evaporation and dehydration system 7 and dewaters, and the head temperature of described evaporation and dehydration system 7 is 110 ℃, pressure is 0.4MPa (absolute pressure), bottom temp is 210 ℃, and pressure is 0.45MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; Extraction treated oil in bottom is as the charging of reactor 2-3, and the boiling range of gained treated oil is 75-186 ℃, sulphur content trace (can not detecting), non-aromatics content is 98.8% (m), aromaticity content is 1.2% (m), and octane value (RON) is that 63,20 ℃ of density are 738 kilograms/meter
3A gained treated oil part is as raffinating oil (f) extraction, and its flow is 0.940 ton/hour, and it can be used as gasoline mediation product; Total liquid yield is 80.44%; Another part treated oil, its flow are 3.279 tons/hour, react through entering reactor 2-3 after the process furnace 1-3 heating, and 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.
In the utility model total liquid yield equal BTX aromatics, petroleum naphtha, benzene and the flow sum of raffinating oil divided by the raw material inlet amount.
Aromatics yield equals the BTX aromatics flow and multiply by aromaticity content and add that the flow of benzene is 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 0.378 ton/hour, and pure hydrogen flow is 0.344 ton/hour, and hydrogen yield is 2.75% (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 1.012 tons/hour; Described stabilizer tower system side line extraction mouth temperature is 129 ℃, and pressure is 0.96MPa (absolute pressure), extraction petroleum naphtha (g); The boiling range of described petroleum naphtha is 35-75 ℃, and sulphur content trace (can not detecting), non-aromatics content are 99.8% (m), and aromaticity content is 0.2% (m), and octane value (RON) is that 70,20 ℃ of density are 571 kilograms/meter
3, flow is 1.320 tons/hour, it not only can be used as gasoline mediation product but also can be used as the cracking of ethylene raw material; Gained reformed oil (boiling range is 75-194 ℃) enters extraction system 8 and handles at the bottom of described stabilizer tower system 6 towers, the service temperature of described extraction system 8 is 120 ℃, and working pressure is 0.8MPa (absolute pressure), and solvent ratio is 5, return and wash than being 0.7, 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 (absolute pressure), and column bottom temperature is 175 ℃, and pressure is 0.2MPa (absolute pressure); Top extraction benzene (h), 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 0.401 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 (absolute pressure); 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 80-194 ℃, sulphur content trace (can not detecting), non-aromatics content is 1.9% (m), and aromaticity content is 98.1% (m), and benzene content is 0.57% (m), octane value (RON) is that 131,20 ℃ of density are 862 kilograms/meter
3, flow is 7.810 tons/hour, aromatics yield is 64.50% (weight); The bottom production returns and enters extraction system; Through after extraction system 8 extractings, raffinate oil top through extraction system 8 of gained enters evaporation and dehydration system 7 and dewaters, and the head temperature of described evaporation and dehydration system 7 is 120 ℃, pressure is 0.5MPa (absolute pressure), bottom temp is 225 ℃, and pressure is 0.55MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; Bottom extraction treated oil (as the charging of the second reactor 2-2), the boiling range of gained treated oil is 75-184 ℃, sulphur content trace (can not detecting), non-aromatics content is 98.7% (m), aromaticity content is 1.3% (m), and octane value (RON) is that 63,20 ℃ of density are 740 kilograms/meter
3; A gained treated oil part is as raffinating oil (f) extraction, and its flow is 1.579 tons/hour, and it can be used as gasoline mediation product; Total liquid yield is 88.88%; Another part treated oil, its flow are 3.291 tons/hour, and through entering reactor 2-2 and react after the heating, 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 0.336 ton/hour, and pure hydrogen flow is 0.310 ton/hour, and hydrogen yield is 2.48% (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 0.558 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; 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 (absolute pressure), and column bottom temperature is 175 ℃, and pressure is 0.25MPa (absolute pressure); Top extraction benzene (g), 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 0.294 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 (absolute pressure); 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), and aromaticity content is 98.2% (m), and benzene content is 0.38% (m), octane value (RON) is that 134,20 ℃ of density are 865 kilograms/meter
3, flow is 8.434 tons/hour, aromatics yield is 68.61% (weight); The bottom production returns and enters extraction system; Through after extraction system 8 extractings, raffinate oil top through extraction system 8 of gained enters evaporation and dehydration system 7 and dewaters, and the head temperature of described evaporation and dehydration system 7 is 130 ℃, pressure is 0.6MPa (absolute pressure), bottom temp is 240 ℃, and pressure is 0.65MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; 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), and octane value (RON) is 64, is 745 kilograms/meter 20 ℃ of density
3, a gained treated oil part is as raffinating oil (f) extraction, and its flow is 2.879 tons/hour, and it can be used as gasoline mediation product; Total liquid yield is 92.85%; Another part treated oil, its flow are 3.461 tons/hour, react through entering reactor 2-2 after the process furnace 1-2 heating, and 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, described extraction system links to each other with first and second recovery towers again, described evaporation and dehydration system is connected with the 3rd and/or the 4th reaction unit again, and described stabilizer tower system is provided with 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, and described stabilizer tower system is provided with side line extraction mouth; Described extraction system is connected with evaporation and dehydration system by pipeline on the one hand; Described extraction system is connected with first recovery column by pipeline on the other hand; Described first recovery column top is by pipeline extraction benzene, and the bottom is connected with second recovery column by pipeline; Described second recovery column top is by pipeline extraction BTX aromatics, and the bottom is connected with extraction system by pipeline; Described evaporation and dehydration system top is by the pipeline recovered water, and described evaporation and dehydration system bottom is connected with another reaction unit by pipeline and heating unit on the one hand, raffinates oil by the pipeline extraction on the other hand in described evaporation and dehydration system bottom; 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, is connected with described high-pressure separator then.
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 |
|---|---|---|---|
| CN2009201091869U CN201459036U (en) | 2009-06-17 | 2009-06-17 | Naphtha reforming system for producing raffinate oil, benzene and mixed aromatics |
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| CN2009201091869U CN201459036U (en) | 2009-06-17 | 2009-06-17 | Naphtha reforming system for producing raffinate oil, benzene and mixed aromatics |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101921620A (en) * | 2009-06-17 | 2010-12-22 | 北京金伟晖工程技术有限公司 | Naphtha reforming system and method for producing raffinate oil, benzene and mixed aromatic hydrocarbons |
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2009
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101921620A (en) * | 2009-06-17 | 2010-12-22 | 北京金伟晖工程技术有限公司 | Naphtha reforming system and method for producing raffinate oil, benzene and mixed aromatic hydrocarbons |
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