CN102002389B - Naphtha prolific aromatics reforming system with lateral line cutting system and recovery system and naphtha prolific aromatics reforming method - Google Patents
Naphtha prolific aromatics reforming system with lateral line cutting system and recovery system and naphtha prolific aromatics reforming method Download PDFInfo
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- CN102002389B CN102002389B CN200910089241.7A CN200910089241A CN102002389B CN 102002389 B CN102002389 B CN 102002389B CN 200910089241 A CN200910089241 A CN 200910089241A CN 102002389 B CN102002389 B CN 102002389B
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- 238000000034 method Methods 0.000 title claims abstract description 62
- 238000011084 recovery Methods 0.000 title claims abstract description 49
- 238000002407 reforming Methods 0.000 title claims abstract description 31
- 230000002062 proliferating effect Effects 0.000 title abstract 6
- 238000000605 extraction Methods 0.000 claims abstract description 93
- 238000006243 chemical reaction Methods 0.000 claims abstract description 66
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 45
- 238000010438 heat treatment Methods 0.000 claims abstract description 35
- 239000003502 gasoline Substances 0.000 claims abstract description 18
- 239000002904 solvent Substances 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 22
- 238000009835 boiling Methods 0.000 claims description 20
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- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical group O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 claims description 3
- UWHCKJMYHZGTIT-UHFFFAOYSA-N tetraethylene glycol Chemical compound OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 claims description 3
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 26
- 239000001257 hydrogen Substances 0.000 abstract description 26
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 25
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 abstract description 13
- 239000007788 liquid Substances 0.000 abstract description 11
- 238000012545 processing Methods 0.000 abstract description 9
- 238000001833 catalytic reforming Methods 0.000 abstract description 8
- 230000006641 stabilisation Effects 0.000 abstract 1
- 238000011105 stabilization Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 71
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 17
- 239000003054 catalyst Substances 0.000 description 14
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- 150000001335 aliphatic alkanes Chemical class 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
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- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 3
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Abstract
The invention discloses a naphtha prolific aromatics reforming system and a naphtha prolific aromatics reforming method. The reforming system comprises a heating device and a reaction device connected with the heating device and is characterized in that: the reaction device is divided into two parts; the first reaction device and/or the second reaction device are connected with each other through a high-pressure separation device, a stabilization tower system, an extraction system and a raffinate oil cutting system; the extraction system is connected with a recovery system; the raffinate oil cutting system is connected with a lateral line cutting tower; and the lateral line cutting tower is connected with the third reaction device and/or the fourth reaction device. Compared with the conventional catalytic reforming process, the naphtha prolific aromatics reforming system and the naphtha prolific aromatics reforming method have the advantages that: under lower pressure, products after a reaction are extracted and are subjected to raffinate oil cutting to generate refined oil and the generated refined oil is mixed with recycle hydrogen to enter another reactor to further react, so that processing capacity of the system is improved, processing capacity of the system is improved and the liquid yield, the aromatics yield and the hydrogen yield are greatly increased; and a high octane value product is provided and a solvent is recovered by using a recovery tower, so that benzene is separated from the mixed aromatics, the types of the products are increased, the benzene content of the mixed aromatics is reduced, and the benzene content of blended gasoline is further reduced.
Description
Technical field
The present invention relates to a kind of catalytic reforming and method thereof, particularly a kind of naphtha fecundation aromatic hydrocarbons reforming system with side line diced system and recovery system and method thereof.
Background technology
Fast development and the growth of petrochemical industry to aromatic hydrocarbons demand along with automotive industry; the particularly increasingly stringent requirement of country to environment protection, catalytic reforming gasoline becomes one of blend component desirable in New standard gasoline with its high-octane rating, low alkene and Trace Sulfur.A large amount of hydrogen of catalytic reforming by product are again for improving oil quality, and the industry of development hydrogenation provides a large amount of cheap hydrogen sources.Therefore, catalytic reforming, as the important oil refining process of producing stop bracket gasoline and aromatic hydrocarbons, is being brought into play more and more important effect in oil refining, chemical engineering industry.
Catalytic reforming unit is pressed catalyst regeneration mode, mainly can be divided at present semi-regenerative reforming and CONTINUOUS REFORMER two classes.Two class catalytic reforming units are because having different separately features, and Bei Ge refinery is selected by its different Raw material processing requirement.
Semi-regenerative reforming is because plant investment is little, flexible operation, and process cost is low, is suitable for the different features such as industrial scale, still takies critical role.
Since platinum/rhenium catalyst comes out, the research of semi-regenerative reforming catalyzer and application have obtained sufficient development, have arrived quite high level.Half-regeneration reformer faces the pressure that expands 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 charging air speed, thereby improve unit capacity, is best method.On the other hand, reformer feed source presents diversified trend, and the secondary processing oil such as the petroleum naphtha of low arene underwater content and coker gasoline proportion in reformer feed strengthens, and the in poor quality trend of reformer feed is more and more obvious.The in poor quality of raw material is had higher requirement to catalyst activity.
Therefore providing a kind of can improve processing power, and naphtha fecundation aromatic hydrocarbons reforming system and the method thereof of raising liquid yield, aromatic production, octane value and hydrogen output just become this technical field urgent need to solve the problem.
Summary of the invention
One of object of the present invention is to provide and a kind ofly can improves processing power, and improves the naphtha fecundation aromatic hydrocarbons reforming system that liquid yield, aromatic production and hydrogen yield provide high-octane rating product simultaneously.
For achieving the above object, the present invention takes following technical scheme:
A naphtha fecundation aromatic hydrocarbons reforming system, comprises heating unit, the reaction unit being attached thereto; It is characterized in that: described reaction unit is divided into two portions, the first and/or second reaction unit connects by high-pressure separation apparatus, stabilizer tower system, extraction system and the diced system of raffinating oil, and described extraction system is also connected with recovery system; The described diced system of raffinating oil is connected with side line Cutting Tap, and described side line Cutting Tap is connected with the 3rd and/or the 4th reaction unit again.
A naphtha fecundation aromatic hydrocarbons reforming system, comprises heating unit, the reaction unit being 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 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 connected with first recovery column by pipeline on the other hand, and first recovery column top is by pipeline extraction benzene, and bottom production is connected with second recovery column by pipeline; Described second recovery column top is by pipeline extraction BTX aromatics, and described second recovery column bottom is connected with extraction system by pipeline; Raffinate oil by pipeline extraction lightweight in the described diced system top of raffinating oil, the described diced system middle part of raffinating oil is connected with side line Cutting Tap by pipeline, described side line Cutting Tap top is connected with the diced system of raffinating oil by pipeline, and described side line Cutting Tap bottom is connected with another reaction unit (the 3rd reaction unit) by pipeline and heating unit; The described cutting unit bottom of raffinating oil is by pipeline extraction kerosene; The other end of described another reaction unit is connected with described high-pressure separator by pipeline.
An optimal technical scheme, is characterized in that: described reaction unit is first connected with the second reaction unit by second heating unit, and then is connected with described high-pressure separator.
An optimal technical scheme, is characterized in that: described another reaction unit is first connected with the 4th reaction unit by the 4th heating unit, and then is connected with described high-pressure separator.
An optimal technical scheme, is characterized in that: two reactors of described reaction unit for connecting up and down, are connected by heating unit therebetween.
An optimal technical scheme, is characterized in that: two reactors of described another reaction unit for connecting up and down, are connected by heating unit therebetween.
Another object of the present invention is to provide raising processing power, and improves the naphtha productive aromatic hydrocarbon reforming method that liquid yield, aromatic production and hydrogen yield provide high-octane rating product simultaneously.
Foregoing invention object of the present invention reaches by the following technical programs:
A naphtha productive aromatic hydrocarbon reforming method, its step is as follows: boiling range be the feed naphtha of 80-185 ℃ through after heating unit heating, enter reaction unit and react; The temperature in of described reaction unit is 470-530 ℃, and inlet pressure is 1.0-1.6MPa, and air speed is 3.0-5.0h
-1; Gained reaction product enters high-pressure separator and carries out high pressure separation through overcooling is laggard, and the service temperature of described high-pressure separator is 35-45 ℃, and working pressure is 1.2-1.4MPa; After high pressure separation, a gained hydrogen part is sent outside, and another part is back to reaction unit and another reaction unit through compression set; Gained reformate enters stabilizer tower system and processes, the tower top temperature of described stabilizer tower system is 100-120 ℃, and tower top pressure is 0.8-1.05MPa, and column bottom temperature is 220-240 ℃, tower bottom pressure is 0.85-1.10MPa (absolute pressure), and reflux ratio is 0.90-1.15; Overhead extraction water, dry gas and liquefied gas; At the bottom of tower, gained boiling range is that the reformed oil of 71-195 ℃ enters extraction system and processes, and the service temperature of described extraction system is 90-150 ℃, and working pressure is 0.6-1.0MPa, solvent ratio is 3-8, return and wash than being 0.5-1.0, extraction solvent is tetramethylene sulfone, N-formyl morpholine or Tetraglycol 99; After extracting, the extraction oil of extraction system enters first recovery column, and the tower top temperature of described first recovery column is 85-90 ℃, and pressure is 0.1-0.2MPa, and column bottom temperature is 175 ℃, and pressure is 0.1-0.2MPa; Top extraction benzene, bottom production enters second recovery column, and the tower top temperature of described second recovery column is 110-155 ℃, and pressure is 0.02-0.05MPa, and column bottom temperature is 175 ℃, pressure is 0.02-0.05MPa; Top extraction BTX aromatics, partly or entirely as gasoline blend component, bottom production refluxes and enters extraction system; After extracting, raffinating oil of described extraction system enters the Cutting Tap cutting of raffinating oil, described in the raffinate oil head temperature of Cutting Tap be 75-95 ℃, pressure is 0.1-0.2MPa, bottom temp is 175-213 ℃, and pressure is 0.13-0.23MPa, and reflux ratio is 20-60; Bottom extraction kerosene, top extraction lightweight is raffinated oil; It is 100-140 ℃ that the side line of the described Cutting Tap of raffinating oil is adopted temperature out, and pressure is 0.11-0.21MPa, and extraction treated oil enters side line Cutting Tap; The condition of described side line Cutting Tap is that tower top temperature is 80-99 ℃, and pressure is 0.1-0.2MPa, and column bottom temperature is 180-218 ℃, and pressure is 0.13-0.23MPa; The Cutting Tap of raffinating oil described in top production passes back into, bottom production enters another reaction unit and reacts after heating, and gained reaction product enters high-pressure separator through overcooling is laggard.
An optimal technical scheme, is characterized in that: the reaction product of described reaction unit after the heating of second heating unit, enters the second reaction unit reaction again, and gained reaction product enters high-pressure separator through overcooling is laggard.
An optimal technical scheme, is characterized in that: the reaction product of described another reaction unit after the heating of the 4th heating unit, enters the 4th reaction unit reaction again, and gained reaction product enters high-pressure separator through overcooling is laggard.
Extraction system described in the present invention is that the patent No. is disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation and water wash system.
The system of stabilizer tower described in the present invention and the diced system of raffinating oil are conventional system, comprise tower, air-cooler, watercooler, return tank, reflux pump and column bottoms pump etc.
Process furnace described in the present invention and condensing works are conventional device.
Used catalyst described in the present invention in reactor is conventional reforming catalyst.
Beneficial effect:
The advantage of naphtha fecundation aromatic hydrocarbons reforming system of the present invention and method thereof is: compare with existing catalytic reforming process, in naphtha fecundation aromatic hydrocarbons reforming system of the present invention and method, under lower pressure, reacted product through extracting and raffinate oil cutting after, after the treated oil generating mixes with recycle hydrogen, entering another reactor further reacts, the processing power of system of the present invention is improved, liquid yield, aromatic production and hydrogen yield improve greatly, high-octane rating product is provided simultaneously, and owing to having adopted recovery tower to carry out solvent recuperation, benzene in BTX aromatics is separated, not only increased product category, and reduced the benzene content in BTX aromatics, and then the benzene content in blended gasoline is further reduced.
Below by the drawings and specific embodiments, the present invention will be further described, but and do not mean that limiting the scope of the invention.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the embodiment of the present invention 1.
Fig. 2 is the schematic flow sheet of the embodiment of the present invention 2.
Fig. 3 is the schematic flow sheet of the embodiment of the present invention 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the embodiment of the present invention 1.By boiling range, be 80-185 ℃, sulphur content is 0.5ppm, nitrogen content 0.5ppm, metal content is 5ppb, water content 5ppm, and Determination of Alkane Content is 70% (m), naphthene content is 28% (m), aromaticity content is 2% (m), and octane value (RON) is that 42,20 ℃ of density are 732 kgs/m
3, flow is that the feed purification petroleum naphtha of 12.5 tons/hour first passes through heat exchange, then after process furnace 1-1 heating, enters reactor 2-1 and react, air speed (air speed equals feed purification petroleum naphtha divided by the cumulative volume of catalyzer) is 3.0h
-1, the temperature in of described reactor 2-1 is 470 ℃, and inlet pressure is 1.0MPa (absolute pressure), go out gained reaction product after process furnace 1-2 heating, enter reactor 2-2 and react, the temperature in of described reactor 2-2 is 470 ℃, and inlet pressure is 1.0MPa (absolute pressure), through heat exchange and condenser 3, enter high-pressure separator 4 after cooling and carry out high pressure separation, the service temperature of described high-pressure separator 4 is 35 ℃, and working pressure is 1.2MPa (absolute pressure), after high pressure separation, a gained hydrogen wherein part is sent outside, flow is 0.371 ton/hour, producing hydrogen rate is 2.97%, other hydrogen is back to process furnace 1-1 and process furnace 1-3 through compressor 5, the hydrogen to oil volume ratio being wherein back to before process furnace 1-1 is 800: 1, and the hydrogen to oil volume ratio entering before process furnace 1-3 is 1200: 1 (before entering process furnace, first carrying out heat exchange), through high-pressure separator 4 gained reformates, entering stabilizer tower system 6 processes, the tower top temperature of described stabilizer tower system 6 is 100 ℃, tower top pressure is 0.8MPa (absolute pressure), column bottom temperature is 220 ℃, tower bottom pressure is 0.85MPa (absolute pressure), and reflux ratio (m/m) is 0.90, overhead extraction water, dry gas and liquefied gas, its flow is 0.684 ton/hour, gained reformed oil at the bottom of tower (boiling range is 35-191 ℃) enters extraction system 8 and processes, and the temperature of described extraction system 8 is 100 ℃, and working pressure is 0.6MPa (absolute pressure), and solvent ratio is 3, returns and washes than being 0.5, and solvent for use is tetramethylene sulfone, after extracting, gained is extracted oil out and is entered first recovery column 9-1, the tower top temperature of described first recovery column 9-1 is 85 ℃, pressure is 0.1MPa (absolute pressure), column bottom temperature is 175 ℃, the products benzene of 0.311 ton/hour of the direct extraction in top of described first recovery column 9-1, freezing point can reach 5.4 ℃, the mixture of the bottom extraction of described first recovery column 9-1 enters second recovery column 9-2, the tower top temperature of described second recovery column 9-2 is 110 ℃, pressure is 0.02MPa (absolute pressure), column bottom temperature is 175 ℃, the BTX aromatics of 6.684 tons/hour of the direct extraction in top of described second recovery column 9-2, the boiling range of gained BTX aromatics is 80-193 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 2.0% (m), aromaticity content is 98% (m), octane value (RON) is 128, 20 ℃ of density are 858 kgs/m
3, aromatics yield is 56.42 % by weight, and this BTX aromatics is the gasoline blend component of high-quality, and the extraction solvent of described second recovery column bottom extraction enters extraction system 8 tops by backflow, after extracting, gained is raffinated oil and through top, is entered the Cutting Tap 7-1 that raffinates oil and carry out cutting and separating, the head temperature of the described Cutting Tap 7-1 that raffinates oil is 75 ℃, pressure is 0.1MPa (absolute pressure), bottom temp is 175 ℃, pressure is 0.13MPa (absolute pressure), and reflux ratio (m/m) is 20, bottom extraction kerosene, the boiling range of gained kerosene is 145-191 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 97.0% (m),, aromaticity content is 3.0% (m), 20 ℃ of density are 766 kgs/m
3, cetane value is 40, flow is 1.976 tons/hour, can be used as the gasoline blend component of high-quality, top extraction lightweight is raffinated oil, and the boiling range that gained lightweight is raffinated oil is 35-80 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 99.8% (m), aromaticity content is 0.2% (m), and octane value (RON) is that 71,20 ℃ of density are 685 kgs/m
3, flow is 2.875 tons/hour, is the gasoline blend component of high-quality, total liquid yield is 91.55%.The described Cutting Tap 7-1 that raffinates oil is provided with side line extraction mouth, it is 100 ℃ that this side line is adopted temperature out, pressure is 0.11MPa (absolute pressure), extraction treated oil (as side line Cutting Tap 7-2 charging), the refining oil plant of gained carries out cutting and separating through top side line approaching side line Cutting Tap 7-2, and the head temperature of described Cutting Tap 7-2 is 80 ℃, and pressure is 0.1MPa (absolute pressure), bottom temp is 180 ℃, and pressure is 0.13MPa (absolute pressure); Described side line Cutting Tap 7-2 top extraction is gently raffinated oil, and enters by backflow the Cutting Tap 7-1 that raffinates oil; Described side line Cutting Tap 7-2 bottom extraction heavily raffinate oil (flow is 5.068 tons/hour) as raw material, after process furnace 1-3 heating, enter reactor 2-3 and react, the temperature in of described reactor 2-3 is 470 ℃, inlet pressure is 1.0MPa (absolute pressure), gained reaction product enters reactor 2-4 reaction after process furnace 1-4 heating, the temperature in of described reactor 2-4 is 470 ℃, and inlet pressure is 1.0MPa (absolute pressure); Gained reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling after mixing with the reaction product of described reactor 2-2.
Wherein each reactor packs the ratio of catalytic amount into and is:
Reactor 2-1: reactor 2-2: reactor 2-3: reactor 2-4=1: 1.5: 2: 3.5.
The present invention's reforming catalyst used is a kind of Pt, Re reforming catalyst, the mono-diaspore of GM and the mono-diaspore of Ziegler synthesising by-product SB that its carrier is made for employing aluminium colloidal sol deep fat ageing process mix by a certain percentage, the compound γ-aluminium sesquioxide that has two concentrated Kong Feng making through moulding, roasting.On catalyzer, Pt content is 0.10～1.00 heavy %, and Re content is 0.10～3.00 heavy %, and Cl content is 0.50～3.00 heavy %, and this catalyzer has the feature of high reactivity, highly selective and low carbon deposit.
In the present invention, total liquid yield equals flow sum that benzene, BTX aromatics, kerosene and lightweight raffinate oil divided by raw material inlet amount.
Aromatics yield equals BTX aromatics flow and is multiplied by aromaticity content and benzene flow sum again divided by raw material inlet amount.
Hydrogen yield equals outer row's hydrogen amount and is multiplied by hydrogen purity again divided by raw material inlet amount.
The physico-chemical property of reactor 2-1 and 2-2 used catalyst 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 used catalyst 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 present invention's measuring method used is (lower same):
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 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 oil: the standard test methods of nickel, vanadium and iron in ASTM D 5708-2005 inductively coupled plasma (ICP) aes determination crude oil and trapped fuel;
10, nitrogen content: 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 present invention 2.By boiling range, be 80-185 ℃, sulphur content is 0.54ppm, nitrogen content 0.5ppm, metal content is 5ppb, water content 5ppm, and Determination of Alkane Content is 60% (m), naphthene content is 34% (m), aromaticity content is 6% (m), and octane value (RON) is that 50,20 ℃ of density are 738 kgs/m
3, flow is that the feed purification petroleum naphtha of 12.5 tons/hour first passes through heat exchange, then after process furnace 1-1 heating, enters reactor 2-1 and react, air speed (air speed equals feed purification petroleum naphtha divided by the cumulative volume of catalyzer) is 4.0h
-1, described reactor 2-1 by reactor 2-1 under upper and reactor 2-1 two reactors in series form, two reactors are connected by process furnace 1-2, the temperature in of described reactor 2-1 above and under reactor 2-1 is 480 ℃, and inlet pressure is 1.3MPa (absolute pressure), through products therefrom after reactor 2-1 reaction, through heat exchange and condenser 3, enter high-pressure separator 4 after cooling and carry out high pressure separation, the service temperature of described high-pressure separator 4 is 40 ℃, and working pressure is 1.3MPa (absolute pressure), after high pressure separation, a gained hydrogen wherein part is sent outside, flow is 0.393 ton/hour, other hydrogen is back to process furnace 1-1 and process furnace 1-3 through compressor 5, the hydrogen to oil volume ratio being wherein back to before process furnace 1-1 is 800: 1, and the hydrogen to oil volume ratio entering before process furnace 1-3 is 1200: 1 (before entering process furnace, first carrying out heat exchange), through high-pressure separator 4 gained reformates, entering stabilizer tower system 6 processes, the tower top temperature of described stabilizer tower 6 is 102 ℃, and tower top pressure is 0.95MPa (absolute pressure), and column bottom temperature is 230 ℃, tower bottom pressure is 1.0MPa (absolute pressure), and reflux ratio (m/m) is 0.99, overhead extraction water, dry gas and liquefied gas, its flow is 1.061 tons/hour, gained reformed oil at the bottom of tower (boiling range is 35-205 ℃) enters extraction system 8 and processes, 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 0.75, solvent for use is N-formyl morpholine, after extracting, gained is extracted oily portion out and is entered first recovery column 9-1, the head temperature of described first recovery column is 87 ℃, pressure is 0.15MPa (absolute pressure), bottom temp is 175 ℃, pressure is 0.15MPa (absolute pressure), the products benzene that the direct extraction in described first recovery column bottom is 0.41 ton/hour, freezing point can reach 5.4 ℃, the mixture of described first recovery column bottom extraction enters second recovery column 9-2, the head temperature of described second recovery column is 130 ℃, pressure is 0.035MPa (absolute pressure), bottom temp is 175 ℃, pressure is 0.035MPa (absolute pressure), the BTX aromatics that the direct extraction in described second recovery column top is 8.041 tons/hour, the boiling range of gained BTX aromatics is 80-207 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 1.9% (m), aromaticity content is 98.1% (m), octane value (RON) is 130, 20 ℃ of density are 862 kgs/m
3, aromatics yield is 64.11 % by weight, after cutting, is the gasoline blend component of high-quality, the extraction solvent of described second recovery column bottom extraction enters extraction system 8 tops by backflow, after extracting, gained is raffinated oil and through top, is entered the Cutting Tap 7-1 that raffinates oil and carry out cutting and separating, the head temperature of the described Cutting Tap 7-1 that raffinates oil is 92 ℃, pressure is 0.15MPa (absolute pressure), bottom temp is 194 ℃, pressure is 0.18MPa (absolute pressure), and reflux ratio (m/m) is 30, bottom extraction kerosene, the boiling range of gained kerosene is 155-205 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 98.6% (m), and aromaticity content is 1.4% (m), and 20 ℃ of density are 773 kgs/m
3, cetane value is 42, flow is 0.795 ton/hour, can be used as the gasoline blend component of high-quality, top extraction lightweight is raffinated oil, and the boiling range that gained lightweight is raffinated oil is 35-85 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 99.89% (m), aromaticity content is 0.11% (m), and octane value (RON) is that 70,20 ℃ of density are 611 kgs/m
3, flow is 1.8 tons/hour, is the gasoline blend component of high-quality, total liquid yield is 88.33 % by weight, the described Cutting Tap 7-1 that raffinates oil is provided with side line extraction mouth, and it is 120 ℃ that this side line is adopted temperature out, and pressure is 0.16MPa (absolute pressure), extraction treated oil (as side line Cutting Tap 7-2 charging), the refining oil plant of gained enters side line Cutting Tap 7-2 through top and carries out cutting and separating, and the head temperature of described side line Cutting Tap 7-2 is 92 ℃, and pressure is 0.15MPa (absolute pressure), and bottom temp is 200 ℃, and pressure is 0.18MPa (absolute pressure), described side line Cutting Tap 7-2 top extraction is gently raffinated oil and is entered by backflow the Cutting Tap 7-1 that raffinates oil, described side line Cutting Tap 7-2 bottom extraction heavily raffinate oil (flow is 1.231 tons/hour) as raw material after process furnace 1-3 heating, entering reactor 2-2 reacts, described reactor 2-2 by reactor 2-2 under upper and reactor 2-2 two reactors in series form, between by process furnace 1-4, be connected, the temperature in of described reactor 2-2 above and under reactor 2-2 is 480 ℃, and inlet pressure is 1.3MPa (absolute pressure), gained reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling.
Wherein reactor 2-1 is upper: under reactor 2-1: reactor 2-2 is upper: under reactor 2-2=1: 1.5: 2: 3.5.
The physico-chemical property of reactor 2-1 used catalyst 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 used catalyst 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 |
[0060]embodiment 3
As shown in Figure 3, be the schematic flow sheet of the embodiment of the present invention 3.By boiling range, be 80-185 ℃, sulphur content is 0.45ppm, nitrogen content 0.5ppm, metal content is 5ppb, water content 5ppm, and Determination of Alkane Content is 47% (m), naphthene content is 42% (m), aromaticity content is 11% (m), and octane value (RON) is that 61,20 ℃ of density are 742 kgs/m
3, flow is that the refining petroleum naphtha of 12.5 tons/hour first passes through heat exchange, then after process furnace 1-1 heating, enters reactor 2-1 and react, air speed (air speed equals feed purification petroleum naphtha divided by the cumulative volume of catalyzer) is 5.0h
-1, the temperature in of described reactor 2-1 is 530 ℃, and inlet pressure is 1.6MPa (absolute pressure), gained reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling and carries out high pressure separation, and the service temperature of described high-pressure separator 4 is 45 ℃, and working pressure is 1.4MPa (absolute pressure), after high pressure separation, a gained hydrogen wherein part is sent outside, flow is 0.522 ton/hour, producing hydrogen rate is 4.17%, other hydrogen is back to process furnace 1-1 and process furnace 1-2 through compressor 5, the hydrogen to oil volume ratio being wherein back to before process furnace 1-1 is 800: 1, and the hydrogen to oil volume ratio entering before process furnace 1-2 is 1200: 1 (before entering process furnace, first carrying out heat exchange), through high-pressure separator 4 gained reformates, entering stabilizer tower tower 6 processes, the tower top temperature of described stabilizer tower 6 is 120 ℃, and tower top pressure is 1.05MPa (absolute pressure), and column bottom temperature is 240 ℃, tower bottom pressure is 1.10MPa (absolute pressure), and reflux ratio (m/m) is 1.15, overhead extraction water, dry gas and liquefied gas, its flow is 1.39 tons/hour, gained reformed oil at the bottom of tower (boiling range is 35-220 ℃) enters extraction system 8 and processes, the service temperature of described extraction system 8 is 150 ℃, and working pressure is 1.0MPa (absolute pressure), and solvent ratio is 8, return and wash than being 1.0, solvent for use is Tetraglycol 99, after extracting, gained is extracted oil out and is entered first recovery column 9-1, the head temperature of described first recovery column is 90 ℃, pressure is 0.2MPa (absolute pressure), bottom temp is 175 ℃, pressure is 0.2MPa (absolute pressure), the products benzene that the direct extraction in described first recovery column bottom is 1.006 tons/hour, freezing point can reach 5.4 ℃, the mixture of described first recovery column bottom extraction enters second recovery column 9-2, the head temperature of described second recovery column is 155 ℃, pressure is 0.05MPa (absolute pressure), bottom temp is 175 ℃, pressure is 0.05MPa (absolute pressure), the BTX aromatics that the direct extraction in described second recovery column top is 7.752 tons/hour, the boiling range of gained BTX aromatics is 80-223 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 1.8% (m), aromaticity content is 98.2% (m), octane value (RON) is 135, 20 ℃ of density are 869 kgs/m
3, aromatics yield is 70.07 % by weight, and this BTX aromatics is the gasoline blend component of high-quality after cutting, and the extraction solvent of described recovery tower bottom extraction enters extraction system 8 tops by backflow, after extracting, gained is raffinated oil and through top, is entered the Cutting Tap 7-1 that raffinates oil and carry out cutting and separating, the head temperature of the described Cutting Tap 7-1 that raffinates oil is 95 ℃, pressure is 0.2MPa (absolute pressure), bottom temp is 213 ℃, pressure is 0.23MPa (absolute pressure), and reflux ratio (m/m) is 60, bottom extraction kerosene, the boiling range of gained kerosene is 165-220 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 98.3% (m), and aromaticity content is 1.7% (m), and 20 ℃ of density are 786 kgs/m
3, flow is 0.79 ton/hour, after cutting, is the gasoline blend component of high-quality, top extraction lightweight is raffinated oil, and the boiling range that gained lightweight is raffinated oil is 35-90 ℃, sulphur content trace (inspection does not measure), Determination of Alkane Content is 99.88% (m), aromaticity content is 0.12% (m), and octane value (RON) is that 70,20 ℃ of density are 623 kgs/m
3, cetane value is 44, flow is 1.039 tons/hour, can be used as the gasoline blend component of high-quality, total liquid yield is 84.69 % by weight, the described Cutting Tap 7-1 that raffinates oil is provided with side line extraction mouth, and it is 140 ℃ that this side line is adopted temperature out, and pressure is 0.21MPa (absolute pressure), extraction treated oil (as side line Cutting Tap 7-2 charging), the refining oil plant of gained enters side line Cutting Tap 7-2 through top and carries out cutting and separating, and the head temperature of described Cutting Tap 7-2 is 99 ℃, and pressure is 0.2MPa (absolute pressure), and bottom temp is 218 ℃, and pressure is 0.23MPa (absolute pressure), described side line Cutting Tap 7-2 top extraction is gently raffinated oil and is entered by backflow the Cutting Tap 7-1 that raffinates oil, described side line Cutting Tap 7-2 bottom extraction heavily raffinate oil (flow is 2.572 tons/hour) as raw material, after process furnace 1-2 heating, enter reactor 2-2 and react, the temperature in of described reactor 2-2 is 530 ℃, and inlet pressure is 1.6MPa (absolute pressure), gained reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling.
Reactor 2-1: reactor 2-2=1: 2 wherein.
The physico-chemical property of reactor 2-1 used catalyst 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 used catalyst 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 (8)
1. a naphtha fecundation aromatic hydrocarbons reforming system, comprises heating unit, the reaction unit being 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 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 connected with first recovery column by pipeline on the other hand, and first recovery column top is by pipeline extraction benzene, and bottom production is connected with second recovery column by pipeline; Described second recovery column top is by pipeline extraction BTX aromatics, and described second recovery column bottom is connected with extraction system by pipeline; Raffinate oil by pipeline extraction lightweight in the described diced system top of raffinating oil, the described diced system middle part of raffinating oil is connected with side line Cutting Tap by pipeline, described side line Cutting Tap top is connected with the diced system of raffinating oil by pipeline, and described side line Cutting Tap bottom is connected with another reaction unit by pipeline and heating unit; The described cutting unit bottom of raffinating oil is by pipeline extraction kerosene; The other end of described another reaction unit is connected with described high-pressure separator by pipeline.
2. naphtha fecundation aromatic hydrocarbons reforming system according to claim 1, is characterized in that: described reaction unit comprises the first reaction unit and the second reaction unit, and the first reaction unit is connected by secondary heating mechanism with the second reaction unit.
3. naphtha fecundation aromatic hydrocarbons reforming system according to claim 2, is characterized in that: described another reaction unit comprises the 3rd reaction unit and the 4th reaction unit, and the 3rd reaction unit is connected by the 4th heating unit with the 4th reaction unit.
4. naphtha fecundation aromatic hydrocarbons reforming system according to claim 1, is characterized in that: two reactors of described reaction unit for connecting up and down, are connected by heating unit therebetween.
5. naphtha fecundation aromatic hydrocarbons reforming system according to claim 4, is characterized in that: two reactors of described another reaction unit for connecting up and down, are connected by heating unit therebetween.
6. a naphtha productive aromatic hydrocarbon reforming method, its step is as follows: boiling range be the feed naphtha of 80-185 ℃ after heating unit heating, enter reaction unit and react; The temperature in of described reaction unit is 470-530 ℃, and inlet pressure is 1.0-1.6MPa, and air speed is 3.0-5.0h
-1; Gained reaction product enters high-pressure separator and carries out high pressure separation through overcooling is laggard, and the service temperature of described high-pressure separator is 35-45 ℃, and working pressure is 1.2-1.4MPa; After high pressure separation, a gained hydrogen part is sent outside, and another part is back to reaction unit and another reaction unit through compression set; Gained reformate enters stabilizer tower system and processes, and the tower top temperature of described stabilizer tower system is 100-120 ℃, and tower top pressure is 0.8-1.05MPa, and column bottom temperature is 220-240 ℃, and tower bottom pressure is absolute pressure 0.85-1.10MPa, and reflux ratio is 0.90-1.15; Overhead extraction water, dry gas and liquefied gas; At the bottom of tower, gained boiling range is that the reformed oil of 71-195 ℃ enters extraction system and processes, and the service temperature of described extraction system is 90-150 ℃, and working pressure is 0.6-1.0MPa, solvent ratio is 3-8, return and wash than being 0.5-1.0, extraction solvent is tetramethylene sulfone, N-formyl morpholine or Tetraglycol 99; After extracting, the extraction oil of extraction system enters first recovery column, and the tower top temperature of described first recovery column is 85-90 ℃, and pressure is 0.1-0.2MPa, and column bottom temperature is 175 ℃, and pressure is 0.1-0.2MPa; Top extraction benzene, bottom production enters second recovery column, and the tower top temperature of described second recovery column is 110-155 ℃, and pressure is 0.02-0.05MPa, and column bottom temperature is 175 ℃, pressure is 0.02-0.05MPa; Top extraction BTX aromatics, partly or entirely as gasoline blend component, bottom production refluxes and enters extraction system; After extracting, raffinating oil of described extraction system enters the Cutting Tap cutting of raffinating oil, described in the raffinate oil head temperature of Cutting Tap be 75-95 ℃, pressure is 0.1-0.2MPa, bottom temp is 175-213 ℃, and pressure is 0.13-0.23MPa, and reflux ratio is 20-60; Bottom extraction kerosene, top extraction lightweight is raffinated oil; It is 100-140 ℃ that the side line of the described Cutting Tap of raffinating oil is adopted temperature out, and pressure is 0.11-0.21MPa, and extraction treated oil enters side line Cutting Tap; The condition of described side line Cutting Tap is that tower top temperature is 80-99 ℃, and pressure is 0. 1-0.2MPa, and column bottom temperature is 180-218 ℃, and pressure is 0.13-0.23MPa; The Cutting Tap of raffinating oil described in top production passes back into, bottom production enters another reaction unit and reacts after heating, and gained reaction product enters high-pressure separator through overcooling is laggard.
7. naphtha productive aromatic hydrocarbon reforming method according to claim 6, is characterized in that: described reaction unit comprises the first reaction unit and the second reaction unit, and the first reaction unit is connected by secondary heating mechanism with the second reaction unit.
8. naphtha productive aromatic hydrocarbon reforming method according to claim 7, is characterized in that: described another reaction unit comprises the 3rd reaction unit and the 4th reaction unit, and the 3rd reaction unit is connected by the 4th heating unit with the 4th reaction unit.
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Citations (3)
| 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 |
| 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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| CN201459043U (en) * | 2009-07-09 | 2010-05-12 | 北京金伟晖工程技术有限公司 | Naphtha prolificacy arene reforming system with siding cutting system and recycling system |
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Patent Citations (3)
| 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 |
| 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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