CN101935547A - Reforming system and method for increasing caromatic hydrocarbon yield and producing kerosene - Google Patents
Reforming system and method for increasing caromatic hydrocarbon yield and producing kerosene Download PDFInfo
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Abstract
The invention discloses a naphtha caromatic hydrocarbon yield-increasing reforming system and a naphtha caromatic hydrocarbon yield-increasing reforming method. The system comprises a heating device and a reaction unit and is characterized in that: the reaction unit is connected with a high-pressure separator; the high-pressure separator is connected with a stabilizer system; the lower part of the stabilizer system is connected with an extraction system through a pipeline; the extraction system is connected with a raffinate oil cutting system through a pipeline and extracts mixed caromatic hydrocarbon through a pipeline at the same time; the top part of the raffinate oil cutting system is connected with the heating device and another reaction unit (a third reaction unit) through a pipeline, and the lower part of the raffinate oil cutting system extracts the kerosene through a pipeline; and the other end of the another reaction unit is connected with the high-pressure separator through a pipeline. The naphtha caromatic hydrocarbon yield-increasing reforming system and the naphtha caromatic hydrocarbon yield-increasing reforming method of the invention have the advantages of greatly improving processing capability, fluid yield, caromatic hydrocarbon productivity and hydrogen yield.
Description
Technical field
The present invention relates to a kind of reforming system and method thereof, particularly a kind of productive aromatic hydrocarbon is produced the reforming system and the method thereof of kerosene simultaneously.
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 reforming system of liquid yield, aromatic production, octane value and hydrogen output and the difficult problem that method just becomes this technical field urgent need solution thereof.
Summary of the invention
One of purpose of the present invention 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 present invention takes 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 the diced system of raffinating oil by high-pressure separator, stabilizer tower system and extraction system, and the described diced system of raffinating oil is connected with the 3rd and/or the 4th reaction unit (and/or more reaction units) by the top again.
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 stable system by pipeline, and is connected with the raw material supply system by pipeline and compression set; Described stable system bottom is connected with extraction system by pipeline; Described extraction system is connected with the diced system of raffinating oil by pipeline on the one hand; Described extraction system is on the other hand by pipeline extraction BTX aromatics; The described diced system top of raffinating oil is connected with another reaction unit (the 3rd reaction unit) by pipeline and heating unit, and the described diced system bottom of raffinating oil is by pipeline extraction kerosene; 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.
Another object of the present invention provides the raising processing power, and improves the naphtha productive aromatic hydrocarbon reforming method that liquid yield, aromatic production and hydrogen yield provide the high-octane rating product simultaneously.
Foregoing invention purpose of the present invention reaches by the following technical programs:
A kind of naphtha productive aromatic hydrocarbon reforming method, its step is as follows: boiling range is after 80-185 ℃ feed naphtha heats through heating unit, to enter reaction unit and react; The temperature in of described reaction unit is 470-530 ℃, and inlet pressure is 1.0-1.6MPa, and the feed volume air speed is 3.0-5.0h
-1Enter high-pressure separator after the gained reaction product is cooled off through heat exchange and carry out the high pressure separation, the service temperature of described high-pressure separator is 35-45 ℃, and working pressure is 1.2-1.4MPa; After separating through high pressure, a gained hydrogen part is sent outside, and a part is back to feed line and another reaction unit through compression set, and the described hydrogen that returns or advance into pipeline at process furnace perhaps enters pipeline behind process furnace; The gained reformate enters the stabilizer tower system and handles, and the tower top temperature of described stabilizer tower system is 100-120 ℃, and pressure is 0.8-1.05MPa, and column bottom temperature is 220-240 ℃, and pressure is 0.85-1.10MPa, and reflux ratio is 0.90-1.15; Cat head extraction dry gas, liquefied gas and less water; The gained boiling range is that 35-205 ℃ reformed oil enters extraction system and handles at the bottom of the tower, the service temperature of described extraction system is 100-150 ℃, working pressure is 0.6-1.0MPa, solvent ratio is 3.0-8.0, return and wash than being 0.5-1.0, solvent for use is tetramethylene sulfone, N-formyl morpholine, one or more mixing in the Tetraglycol 99; Through after the extracting, the BTX aromatics extraction is as gasoline mediation product or directly as aromatic hydrocarbon product, all the other components enter the diced system of raffinating oil through the top and carry out cutting and separating, the head temperature of the described diced system of raffinating oil is 110-130 ℃, pressure is 0.15-0.25MPa, bottom temp is 180-200 ℃, and pressure is 0.18-0.28MPa, and reflux ratio (m/m) is 20-60; Bottom extraction kerosene, top extraction treated oil, described treated oil enter another reaction unit and react after heating, and the temperature in of described another reaction unit is 470-530 ℃, and inlet pressure is 1.0-1.6MPa, and the feed volume air speed is 1.0-2.0h
-1The gained reaction product enters high-pressure separator after the heat exchange cooling.
A kind of optimal technical scheme, it is characterized in that: the reaction product of described reaction unit is earlier by after second heating unit heating, enter second reaction unit reaction (or connecting more heating unit and corresponding reaction unit behind second reaction unit again), the gained reaction product enters high-pressure separator after cooling off through heat exchange again.
A kind of optimal technical scheme, it is characterized in that: the reaction product of described another reaction unit is earlier by after the 4th the heating unit heating, enter the 4th reaction unit reaction (or connecting more heating unit and corresponding reaction unit behind the 4th reaction unit again), the gained reaction product enters high-pressure separator after cooling off through heat exchange again.
Extraction system described in the present invention 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.
The system of stabilizer tower described in the present invention 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 present invention and condensing works are conventional device.
Catalyst system therefor described in the present invention in the reactor is conventional reforming catalyst.
Beneficial effect:
The advantage of naphtha productive aromatic hydrocarbon reforming system of the present invention and method thereof is: compare with existing catalytic reforming process, in naphtha productive aromatic hydrocarbon reforming system of the present invention and the method, under than low reaction pressure reacted product through extracting and raffinate oil cut 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 invention improve, liquid yield, aromatic production and hydrogen yield improve greatly, and the high-octane rating product is provided simultaneously.
The present invention will be further described below by the drawings and specific embodiments, but and do not mean that limiting the scope of the invention.
Description of drawings
Fig. 1 is the schematic flow sheet of the embodiment of the invention 1.
Fig. 2 is the schematic flow sheet of the embodiment of the invention 2.
Fig. 3 is the schematic flow sheet of the embodiment of the invention 3.
Embodiment
As shown in Figure 1, be the schematic flow sheet of the embodiment of the invention 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 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 2.260 tons/hour; Gained reformed oil at the bottom of the tower (boiling range is 35-205 ℃) 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 75-205 ℃, 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, raffinate oil top through extraction system 8 of gained enters the diced system 7 of raffinating oil and carries out cutting and separating, the head temperature of the described diced system 7 of raffinating oil is 130 ℃, pressure is 0.25MPa (absolute pressure), bottom temp is 200 ℃, pressure is 0.28MPa (absolute pressure), and reflux ratio (m/m) is 20; Bottom extraction kerosene (d), the boiling range of gained kerosene is 160-192 ℃, and sulphur content trace (can not detecting), non-aromatics content are 97% (m), and aromaticity content is 3% (m), and cetane value is that 40,20 ℃ of density are 781 kilograms/meter
3, flow is 0.534 ton/hour; Total liquid yield is 77.21%; Extraction treated oil in top is as the charging of reactor 2-3, and the boiling range of gained treated oil is 35-160 ℃, 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
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 present invention 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 BTX aromatics, kerosene divided by the raw material inlet amount among the present invention.
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:
The physico-chemical property of reactor 2-3 and 2-4 catalyst system therefor is as shown in the table:
The used measuring method of the present invention 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 embodiment of the invention 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 35-200 ℃) 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 75-200 ℃, 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, raffinate oil top through extraction system 8 of gained enters the diced system 7 of raffinating oil and carries out cutting and separating, the head temperature of the described diced system 7 of raffinating oil is 125 ℃, pressure is 0.20MPa (absolute pressure), bottom temp is 195 ℃, pressure is 0.23MPa (absolute pressure), and reflux ratio (m/m) is 40; Bottom extraction kerosene (d), the boiling range of gained kerosene is 160-191 ℃, and sulphur content trace (can not detecting), non-aromatics content are 97.5% (m), and aromaticity content is 2.5% (m), and cetane value is that 41,20 ℃ of density are 779 kilograms/meter
3, flow is 1.418 tons/hour; Total liquid yield is 86.91%; The described diced system top extraction treated oil (as the charging of the second reactor 2-2) of raffinating oil, the boiling range of gained treated oil is 35-160 ℃, 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:
The physico-chemical property of reactor 2-2 catalyst system therefor is as shown in the table:
Embodiment 3
As shown in Figure 3, be the schematic flow sheet of the embodiment of the invention 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 35-196 ℃) 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 75-196 ℃, 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, raffinate oil top through extraction system 8 of gained enters the diced system 7 of raffinating oil and carries out cutting and separating, the head temperature of the described diced system 7 of raffinating oil is 110 ℃, pressure is 0.15MPa (absolute pressure), bottom temp is 180 ℃, pressure is 0.18MPa (absolute pressure), and reflux ratio (m/m) is 60; Bottom extraction kerosene (d), the boiling range of gained kerosene is 160-189 ℃, and sulphur content trace (can not detecting), non-aromatics content are 98% (m), and aromaticity content is 2% (m), and cetane value is that 42,20 ℃ of density are 776 kilograms/meter
3, flow is 2.153 tons/hour; Total liquid yield is 91.71%; The described diced system top extraction treated oil (as the charging of reactor 2-2) of raffinating oil, the boiling range of gained treated oil is 35-160 ℃, 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:
The physico-chemical property of reactor 2-2 catalyst system therefor is as shown in the table:
Claims (9)
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 separator, stabilizer tower system and extraction system, and the described diced system top of raffinating oil is connected with the 3rd and/or the 4th reaction unit again.
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 stable system by pipeline, and is connected with the raw material supply system by pipeline and compression set; Described stable system bottom is connected with extraction system by pipeline; Described extraction system is connected with the diced system of raffinating oil by pipeline on the one hand; Described extraction system is on the other hand by pipeline extraction BTX aromatics; The described diced system top of raffinating oil is connected with another reaction unit by pipeline and heating unit, and the described diced system bottom of raffinating oil is by pipeline extraction kerosene; 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 another 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 reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
7. naphtha productive aromatic hydrocarbon reforming method, its step is as follows: boiling range be 80-185 ℃ feed naphtha through the heating unit heating after, enter reaction unit and react; The temperature in of described reaction unit is 470-530 ℃, and inlet pressure is 1.0-1.6MPa, and the feed volume air speed is 3.0-5.0h
-1Enter high-pressure separator after the gained reaction product is cooled off through heat exchange and carry out the high pressure separation, the service temperature of described high-pressure separator is 35-45 ℃, and working pressure is 1.2-1.4MPa; After separating through high pressure, a gained hydrogen part is sent outside, and a part is back to feed line and another reaction unit through compression set, and the described hydrogen that returns or advance into pipeline at process furnace perhaps enters pipeline behind process furnace; The gained reformate enters the stabilizer tower system and handles, and the tower top temperature of described stabilizer tower system is 100-120 ℃, and pressure is 0.8-1.05MPa, and column bottom temperature is 220-240 ℃, and pressure is 0.85-1.10MPa, and reflux ratio is 0.90-1.15; Cat head extraction dry gas, liquefied gas and less water; The gained boiling range is that 35-205 ℃ reformed oil enters extraction system and handles at the bottom of the tower, the service temperature of described extraction system is 100-150 ℃, working pressure is 0.6-1.0MPa, solvent ratio is 3.0-8.0, return and wash than being 0.5-1.0, solvent for use is tetramethylene sulfone, N-formyl morpholine, one or more mixing in the Tetraglycol 99; Through after the extracting, the BTX aromatics extraction is as gasoline mediation product or directly as aromatic hydrocarbon product, all the other components enter the diced system of raffinating oil through the top and carry out cutting and separating, the head temperature of the described diced system of raffinating oil is 110-130 ℃, pressure is 0.15-0.25MPa, bottom temp is 180-200 ℃, and pressure is 0.18-0.28MPa, and reflux ratio (m/m) is 20-60; Bottom extraction kerosene, top extraction treated oil, described treated oil enter another reaction unit and react after heating, and the temperature in of described another reaction unit is 470-530 ℃, and inlet pressure is 1.0-1.6MPa, and the feed volume air speed is 1.0-2.0h
-1The gained reaction product enters high-pressure separator after the heat exchange cooling.
8. naphtha productive aromatic hydrocarbon reforming method according to claim 7, it is characterized in that: the reaction product of described reaction unit is earlier by after second heating unit heating, enter the reaction of second reaction unit, the gained reaction product enters high-pressure separator after cooling off through heat exchange again.
9. naphtha productive aromatic hydrocarbon reforming method according to claim 8, it is characterized in that: the reaction product of described another reaction unit enters the reaction of the 4th reaction unit by the 4th heating unit earlier, and the gained reaction product enters high-pressure separator after the heat exchange cooling.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3640818A (en) * | 1969-10-31 | 1972-02-08 | Exxon Research Engineering Co | Hydroforming naphthas |
| US4975178A (en) * | 1988-05-23 | 1990-12-04 | Exxon Research & Engineering Company | Multistage reforming with interstage aromatics removal |
| CN1451036A (en) * | 1999-09-27 | 2003-10-22 | 美孚石油公司 | Reformate upgrading using zeolite catalyst |
| CN201241102Y (en) * | 2008-06-04 | 2009-05-20 | 北京金伟晖工程技术有限公司 | Naphtha fecundation aromatic hydrocarbons reforming system |
-
2009
- 2009-07-03 CN CN2009100883850A patent/CN101935547A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3640818A (en) * | 1969-10-31 | 1972-02-08 | Exxon Research Engineering Co | Hydroforming naphthas |
| US4975178A (en) * | 1988-05-23 | 1990-12-04 | Exxon Research & Engineering Company | Multistage reforming with interstage aromatics removal |
| CN1451036A (en) * | 1999-09-27 | 2003-10-22 | 美孚石油公司 | Reformate upgrading using zeolite catalyst |
| CN201241102Y (en) * | 2008-06-04 | 2009-05-20 | 北京金伟晖工程技术有限公司 | Naphtha fecundation aromatic hydrocarbons reforming system |
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Application publication date: 20110105 |