CN102041059B - Reforming system and method with evaporation dehydration system for highly producing high-octane gasoline - Google Patents
Reforming system and method with evaporation dehydration system for highly producing high-octane gasoline Download PDFInfo
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- 230000018044 dehydration Effects 0.000 title claims abstract description 38
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- 230000008020 evaporation Effects 0.000 title claims abstract description 36
- 239000003502 gasoline Substances 0.000 title claims abstract description 29
- 238000002407 reforming Methods 0.000 title claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 63
- 238000000605 extraction Methods 0.000 claims abstract description 54
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- 239000001257 hydrogen Substances 0.000 claims abstract description 26
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- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 claims description 6
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 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
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- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 15
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
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Abstract
The invention discloses a reforming system and a reforming method with an evaporation dehydration system for highly producing high-octane gasoline. The system comprises a heating device and a reaction device, and is characterized in that: the reaction device is divided into two parts; a first reaction device and/or a second reaction device is connected with a raffinate oil cutting system through a high-pressure separation device, a stabilization tower system and an extraction system; the bottom of the raffinate oil cutting system is connected with the evaporation dehydration system; and the evaporation dehydration system is connected with a third reaction device and/or a fourth reaction device. The reforming system and the reforming method with the evaporation dehydration system for highly producing the high-octane gasoline have the advantages that: processing capacity, liquid yield, aromatic hydrocarbon yield and hydrogen yield are greatly improved.
Description
Technical field
The present invention relates to a kind of the catalytic reforming system and method thereof, particularly a kind of reforming system with the evaporation and dehydration system producing high-octane gasoline and method thereof.
Background technology
Along with the fast development of automotive industry and the petrochemical industry growth to the aromatic hydrocarbons demand; 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 the 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 characteristics, the Raw material processing requirement different by it by each refinery and selecting.
Semi-regenerative reforming is because plant investment is little, flexible operation, and process cost is low, is suitable for the different characteristics 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 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, is best method.On the other hand, the 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 the reforming system with the evaporation and dehydration system producing high-octane gasoline 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 purpose of the present invention is to provide and a kind ofly can improves processing power, and improves the reforming system with the evaporation and dehydration system producing high-octane gasoline 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 reforming system with the evaporation and dehydration system producing high-octane gasoline, comprise heating unit, the reaction unit be attached thereto; It is characterized in that: described reaction unit is divided into two portions, the first and/or second reaction unit is connected with the diced system of raffinating oil by high-pressure separation apparatus, stabilizer tower system and extraction system, the described diced system bottom of raffinating oil is connected with evaporation and dehydration system, and described evaporation and dehydration system is connected with the 3rd and/or the 4th reaction unit (and/or more reaction units) again.
A kind of reforming system with the evaporation and dehydration system producing high-octane gasoline, comprise heating unit, the reaction unit be 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 with another reaction unit, is connected with reaction unit by pipeline and compression set; Described stable system bottom is connected with extraction system by pipeline; Described extraction system top is connected with the diced system of raffinating oil by pipeline; Described extraction system bottom extraction BTX aromatics; Raffinate oil by pipeline extraction lightweight in the described diced system top of raffinating oil, the described diced system bottom of raffinating oil is connected with evaporation and dehydration 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 (the 3rd reaction unit); The other end of described another reaction unit is connected with described high-pressure separator by pipeline.
A kind of optimal technical scheme is characterized in that: described reaction unit is by second heating unit be connected with the second reaction unit (can be connected with more reaction unit again by heating unit after the second reaction unit).
A kind of optimal technical scheme is characterized in that: described another reaction unit is by the 4th heating unit be connected with the 4th reaction unit (can be connected with more reaction unit again by heating unit after the 4th reaction unit).
A kind of optimal technical scheme is characterized in that: described reaction unit two (or more than two) reactors for connecting up and down are connected by heating unit therebetween.
A kind of optimal technical scheme is characterized in that: described another reaction unit two (or more than two) reactors for connecting up and down are connected by heating unit therebetween.
Another object of the present invention is to provide the raising processing power, and improves the reforming method with the evaporation and dehydration system producing high-octane gasoline that liquid yield, aromatic production and hydrogen yield provide the high-octane rating product simultaneously.
Above-mentioned purpose of the present invention reaches by the following technical programs:
A kind of reforming method with the evaporation and dehydration system producing high-octane gasoline, its step is as follows: the feed naphtha that boiling range is 80-185 ℃, after the heating unit heating, enters reaction unit and is reacted; 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
-1; The gained reaction product enters high-pressure separator and carries out the high pressure separation after heat exchange is cooling, and the service temperature of described high-pressure separator is 35-45 ℃, and working pressure is 1.2-1.4MPa; After high pressure separates, a gained hydrogen part is sent outside, and a part is back to reaction unit and another reaction unit through compression set, the described hydrogen returned or advance into pipeline at process furnace, or enter pipeline after process furnace; The gained reformate enters the stabilizer tower system and is processed, 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; Overhead extraction dry gas, liquefied gas and a small amount of water; The reformed oil that at the bottom of tower, the gained boiling range is 35-196 ℃ enters extraction system and is processed, 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 that one or more arbitrary proportions in tetramethylene sulfone, N-formyl morpholine or Tetraglycol 99 mix; After the extraction system extracting, extraction BTX aromatics in bottom is as gasoline mediation product or directly as aromatic hydrocarbon product; Raffinate oil and enter diced system cut of raffinating oil in top; The head temperature of the described diced system of raffinating oil is 75-95 ℃, and pressure is 0.1-0.2MPa, and bottom temp is 175-213 ℃, and pressure is 0.13-0.25MPa, and reflux ratio is 20-60; The described diced system top extraction lightweight of raffinating oil is raffinated oil, and bottom extraction heavy is raffinated oil and entered the evaporation and dehydration system dehydration; The head temperature of described evaporation and dehydration system is 110-130 ℃, and pressure is 0.6-0.8MPa, and bottom temp is 210-240 ℃, and pressure is 0.62-0.83MPa; Described evaporation and dehydration system top recovered water, bottom extraction treated oil, after the heating unit heating, enter another reaction unit and reacted; 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 1.0-2.0h
-1; The gained reaction product enters high-pressure separator after heat exchange is cooling.
A kind of optimal technical scheme, it is characterized in that: the reaction product of described reaction unit is first after second heating unit heating, enter the second reaction unit reaction (or connecting again more heating unit and corresponding reaction unit after the second reaction unit), the gained reaction product enters high-pressure separator after heat exchange is cooling again.
A kind of optimal technical scheme, it is characterized in that: the reaction product of described another reaction unit is first after the 4th heating unit heating, enter the 4th reaction unit reaction (or connecting again more heating unit and corresponding reaction unit after the 4th reaction unit), the gained reaction product enters high-pressure separator after heat exchange is cooling again.
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 etc.
The system water of stabilizer tower described in the present invention system is conventional system, comprises 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 the reforming system with the evaporation and dehydration system producing high-octane gasoline of the present invention and method thereof is: with existing catalytic reforming process, compare, in reforming system and method with the evaporation and dehydration system producing high-octane gasoline of the present invention, reacted product is after extracting, raffinate oil cutting and dehydration by evaporation, the treated oil generated 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.
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.
The accompanying drawing explanation
The schematic flow sheet that Fig. 1 is the embodiment of the present invention 1.
The schematic flow sheet that Fig. 2 is the embodiment of the present invention 2.
The schematic flow sheet that Fig. 3 is 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 kg/ms
3, the paraffinic base that flow is 12.5 tons/hour is made with extra care feed naphtha (a) and is first passed through heat exchange, then, after process furnace 1-1 heating, enters reactor 2-1 and reacted, and the feed volume air speed is 3.0h
-1; The temperature in of described reactor 2-1 is 530 ℃, and inlet pressure is 1.0MPa (A, absolute pressure); The gained reaction product, after process furnace 1-2 heating, enters reactor 2-2 and is reacted, and the temperature in of described reactor 2-2 is 530 ℃, and inlet pressure is 1.0MPa (A); Reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling and carries out the high pressure separation, and the service temperature of described high-pressure separator 4 is 35 ℃, and working pressure is 1.2MPa (A); After high pressure separates, a gained hydrogen part is sent (b) outside, and its flow is 0.613 ton/hour, and hydrogen yield is 3.64% (weight); Other hydrogen is back to process furnace 1-1 and process furnace 1-3 through compressor 5, and wherein being back to the front hydrogen to oil volume ratio of process furnace 1-1 is 800: 1, and entering the front hydrogen to oil volume ratio of process furnace 1-3 is 1200: 1 (first carrying out heat exchange before entering process furnace); Entering stabilizer tower system 6 through high-pressure separator 4 gained reformates is processed, the tower top temperature of described stabilizer tower system 6 is 100 ℃, and pressure is 0.8MPa (A), and column bottom temperature is 220 ℃, pressure is 0.85MPa (A), and reflux ratio (m/m) is 0.90; Overhead extraction dry gas, liquefied gas and a small amount of water (c), its flow is 2.401 tons/hour; Gained reformed oil at the bottom of tower (boiling range is 35-196 ℃) enters extraction system 8 and is processed, and the service temperature of described extraction system 8 is 100 ℃, and working pressure is 0.6MPa (A), and solvent ratio is 3.0, returns and washes than being 0.5, and solvent for use is tetramethylene sulfone; After extraction system 8 extractings, 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 (inspection does not measure), 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 kg/ms
3, flow is 9.485 tons/hour, and aromatics yield is 74.36% (weight), and total liquid yield is 75.88%; After extraction system 8 extractings, gained is raffinated oil and is entered through top the diced system 7 of raffinating oil and cut, the head temperature of the described diced system 7 of raffinating oil is 75 ℃, pressure is 0.1MPa (A), bottom temp is 176 ℃, pressure is 0.13MPa (A), and reflux ratio (m/m) is 20; Top extraction lightweight is raffinated oil (d), and the boiling range that described lightweight is raffinated oil is 35-75 ℃, sulphur content trace (inspection does not measure), non-aromatics content is 99.9% (m), aromaticity content is 0.1% (m), and octane value (RON) is that 69,20 ℃ of density are 564 kg/ms
3, flow is 0.534 ton/hour, or it is as gasoline mediation product, or as ethylene cracking material; Total liquid yield is 77.21%; Extraction heavy in bottom is raffinated oil, and flow is 4.292 tons/hour; The gained heavy is raffinated oil and is entered evaporation and dehydration system 9 and dewatered, and described evaporation and dehydration system 9 head temperature are 110 ℃, and pressure is 0.6MPa (A), and bottom temp is 210 ℃, and pressure is 0.62MPa (A); The a small amount of water of top extraction (f), its flow is 0.001 ton/hour; Bottom extraction treated oil (as the charging of reactor 2-3), the boiling range of gained treated oil is 35-186 ℃, sulphur content trace (inspection does not measure), non-aromatics content is 98.8% (m), aromaticity content is 1.2% (m), octane value (RON) is that 63,20 ℃ of density are 738 kg/ms
3, flow is 4.291 tons/hour; The gained treated oil enters reactor 2-3 and is reacted after well heater 1-3 heating, and the temperature in of described reactor 2-3 is 530 ℃, and inlet pressure is 1.0MPa (A); The gained reaction product enters reactor 2-4 reaction after process furnace 1-4 heating, and the temperature in of described reactor 2-4 is 530 ℃, and inlet pressure is 1.0MPa (A), and the feed volume air speed is 1.0h
-1; The gained reaction product with enter high-pressure separator 4 through heat exchange and condenser 3 after cooling after the reaction product of described reactor 2-2 is mixed.
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 present invention's reforming catalyst used is a kind of Pt, Re reforming catalyst, its carrier mixes by a certain percentage for the mono-diaspore of GM and the mono-diaspore of Ziegler synthesising by-product SB that adopts aluminium colloidal sol deep fat ageing process to make, the compound γ-aluminium sesquioxide that two concentrated Kong Feng are arranged made 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 characteristics of high reactivity, highly selective and low carbon deposit.
In the present invention, total liquid yield equals the flow of BTX aromatics divided by the raw material inlet amount.
Aromatics yield equals the BTX aromatics flow and is multiplied by aromaticity content again divided by the raw material inlet amount.
Hydrogen yield equals to efflux the hydrogen amount and is multiplied by hydrogen purity again divided by the 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 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 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: 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 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 kg/ms
3, the intermediate base that flow is 12.5 tons/hour is made with extra care feed naphtha (a) and is first passed through heat exchange, then, after process furnace 1-1 heating, enters reactor 2-1 and reacted; The feed volume air speed is 4.0h
-1, described reactor 2-1 by reactor 2-1 under upper and reactor 2-1 two reactors in series form, be provided with process furnace 1-2 between two reactors, wherein pack into the ratio of catalytic amount of each reactor is that reactor 2-1 goes up: under reactor 2-1=1: 2; The temperature in of described reactor 2-1 is 500 ℃, and inlet pressure is 1.3MPa (A); Enter high-pressure separator 4 through heat exchange and condenser 3 after cooling through products therefrom after reactor 2-1 reaction and carry out the high pressure separation, the service temperature of described high-pressure separator 4 is 40 ℃, and working pressure is 1.3MPa (A); After high pressure separates, a gained hydrogen part is sent (b) outside, and its flow is 0.439 ton/hour, and hydrogen yield is 3.17% (weight); Other hydrogen is after compressor 5 is back to process furnace 1-1 and well heater 1-3, the hydrogen to oil volume ratio wherein be back to after process furnace 1-1 is 800: 1, and the hydrogen to oil volume ratio entered after process furnace 1-3 is 1200: 1 (first carrying out heat exchange before entering reaction unit); Entering stabilizer tower system 6 through high-pressure separator 4 gained reformates is processed, the tower top temperature of described stabilizer tower system 6 is 102 ℃, and pressure is 0.95MPa (A), and column bottom temperature is 227.5 ℃, pressure is 1.00MPa (A), and reflux ratio (m/m) is 0.99; Overhead extraction dry gas, liquefied gas and a small amount of water (c), its flow is 1.198 tons/hour; Gained reformed oil at the bottom of tower (boiling range is 35-194 ℃) enters extraction system 8 and is processed, the service temperature of described extraction system 8 is 120 ℃, and working pressure is 0.8MPa (A), 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, BTX aromatics (e) extraction is as gasoline mediation product or directly as aromatic hydrocarbon product, the boiling range of gained BTX aromatics is 75-194 ℃, sulphur content trace (inspection does not measure), 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 kg/ms
3, flow is 9.445 tons/hour, aromatics yield is 74.12% (weight); After extraction system 8 extractings, gained is raffinated oil and is entered through top the diced system 7 of raffinating oil and cut, the head temperature of the described diced system 7 of raffinating oil is 87 ℃, pressure is 0.15MPa (A), bottom temp is 194 ℃, pressure is 0.18MPa (A), and reflux ratio (m/m) is 40; Top extraction lightweight is raffinated oil (d), and the boiling range that described lightweight is raffinated oil is 35-75 ℃, sulphur content trace (inspection does not measure), non-aromatics content is 99.8% (m), aromaticity content is 0.2% (m), and octane value (RON) is that 70,20 ℃ of density are 571 kg/ms
3, flow is 1.418 tons/hour, it not only can be used as gasoline mediation product but also can be used as ethylene cracking material; Total liquid yield is 86.91%; The described diced system 7 bottom extraction heavys of raffinating oil are raffinated oil, and flow is 4.492 tons/hour; The gained heavy is raffinated oil and is entered evaporation and dehydration system 9 and dewatered, and described evaporation and dehydration system 9 head temperature are 120 ℃, and pressure is 0.7MPa (A), and bottom temp is 225 ℃, and pressure is 0.75MPa (A); The a small amount of water of top extraction (f), its flow is 0.001 ton/hour; Bottom semen collection liquefaction (as the charging of reactor 2-2), the boiling range of gained treated oil is 35-184 ℃, sulphur content trace (inspection does not measure), non-aromatics content is 98.7% (m), aromaticity content is 1.3% (m), octane value (RON) is that 63,20 ℃ of density are 740 kg/ms
3, to be 4.291 tons of/hour gained treated oils enter reactor 2-2 to flow after process furnace 1-3 heating is reacted, and the temperature in of described reactor 2-2 is 500 ℃, and inlet pressure is 1.3MPa (A), and the feed volume air speed is 1.5h
-1; Described reactor 2-2 by reactor 2-2 under upper and reactor 2-2 two reactors in series form, between be provided with process furnace 1-4; Wherein pack into the ratio of catalytic amount of each reactor is that reactor 2-2 is upper: under reactor 2-2=1: 2.5; The gained reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling
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 |
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, Determination of Alkane Content is 47% (m), naphthene content is 42% (m), aromaticity content is 11% (m), octane value (RON) is that 61,20 ℃ of density are 742 kg/m 3, and the cycloalkyl that flow is 12.5 tons/hour is made with extra care petroleum naphtha (a) and first passed through heat exchange, after process furnace 1-1 heating, enter reactor 2-1 and reacted again; The feed volume air speed is 5.0h
-1; The temperature in of described reactor 2-1 is 470 ℃, and inlet pressure is 1.6MPa (A); The gained reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling and carries out the high pressure separation, and the service temperature of described high-pressure separator 4 is 45 ℃, and working pressure is 1.4MPa (A); After high pressure separates, 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 front hydrogen to oil volume ratio of process furnace 1-1 is 800: 1, and entering the front hydrogen to oil volume ratio of process furnace 1-2 is 1200: 1 (first carrying out heat exchange before entering process furnace); Entering stabilizer tower system 6 through high-pressure separator 4 gained reformates is processed, the tower top temperature of described stabilizer tower system 6 is 120 ℃, and pressure is 1.05MPa (A), and column bottom temperature is 240 ℃, pressure is 1.10MPa (A), and reflux ratio (m/m) is 1.15; Overhead extraction dry gas, liquefied gas and a small amount of water (c), its flow is 0.670 ton/hour; Gained reformed oil at the bottom of tower (boiling range is 35-192 ℃) enters extraction system 8 and is processed, and the service temperature of described extraction system 8 is 150 ℃, and working pressure is 1.0MPa (A), and solvent ratio is 8.0, returns and washes than being 1.0, and solvent for use is Tetraglycol 99; After extraction system 8 extractings, gained BTX aromatics (e) extraction is as gasoline mediation product or directly as aromatic hydrocarbon product, the boiling range of gained BTX aromatics is 75-192 ℃, sulphur content trace (inspection does not measure), 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 kg/ms
3, flow is 9.311 tons/hour, aromatics yield is 73.15% (weight); After extraction system 8 extractings, gained is raffinated oil and is entered through top the diced system 7 of raffinating oil and cut, the head temperature of the described diced system 7 of raffinating oil is 95 ℃, pressure is 0.2MPa (A), bottom temp is 213 ℃, pressure is 0.25MPa (A), and reflux ratio (m/m) is 60; Top extraction lightweight is raffinated oil (d), and the boiling range that described lightweight is raffinated oil is 35-75 ℃, sulphur content trace (inspection does not measure), non-aromatics content is 99.7% (m), aromaticity content is 0.3% (m), and octane value (RON) is that 71,20 ℃ of density are 575 kg/ms
3, flow is 2.153 tons/hour, or it is as gasoline mediation product, or as ethylene cracking material; Total liquid yield is 91.71%; The described diced system 7 bottom extraction heavys of raffinating oil are raffinated oil, and flow is 3.959 tons/hour; The gained heavy is raffinated oil and is entered evaporation and dehydration system 9 and dewatered, and described evaporation and dehydration system 9 head temperature are 130 ℃, and pressure is 0.8MPa (A), and bottom temp is 240 ℃, and pressure is 0.83MPa (A); The a small amount of water of top extraction (f), its flow is 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 (inspection does not measure), non-aromatics content is 1.5% (m), aromaticity content is 98.5% (m), octane value (RON) is 64,20 ℃ of density, is 745 kg/ms
3, flow is 4.291 tons/hour; The gained treated oil enters reactor 2-2 and is reacted after process furnace 1-2 heating, and the temperature in of described reactor 2-2 is 470 ℃, and inlet pressure is 1.6MPa (A), and the feed volume air speed is 2.0h
-1; The gained reaction product enters high-pressure separator 4 through heat exchange and condenser 3 after cooling.
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 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 (3)
1. the reforming method with the evaporation and dehydration system producing high-octane gasoline, its step is as follows: the feed naphtha that boiling range is 80-185 ℃, after the heating unit heating, enters reaction unit and is reacted; 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
-1; The gained reaction product enters high-pressure separator and carries out the high pressure separation after heat exchange is cooling, and the service temperature of described high-pressure separator is 35-45 ℃, and working pressure is 1.2-1.4MPa; After high pressure separates, a gained hydrogen part is sent outside, and a part is back to reaction unit and another reaction unit through compression set, the described hydrogen returned or advance into pipeline at process furnace, or enter pipeline after process furnace; The gained reformate enters the stabilizer tower system and is processed, 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; Overhead extraction dry gas, liquefied gas and a small amount of water; The reformed oil that at the bottom of tower, the gained boiling range is 35-196 ℃ enters extraction system and is processed, 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 or Tetraglycol 99; After the extraction system extracting, extraction BTX aromatics in bottom is as gasoline mediation product or directly as aromatic hydrocarbon product; Raffinate oil and enter diced system cut of raffinating oil in top; The head temperature of the described diced system of raffinating oil is 75-95 ℃, and pressure is 0.1-0.2MPa, and bottom temp is 175-213 ℃, and pressure is 0.13-0.25MPa, and reflux ratio is 20-60; The described diced system top extraction lightweight of raffinating oil is raffinated oil, and bottom extraction heavy is raffinated oil and entered the evaporation and dehydration system dehydration; The head temperature of described evaporation and dehydration system is 110-130 ℃, and pressure is 0.6-0.8MPa, and bottom temp is 210-240 ℃, and pressure is 0.62-0.83MPa; Described evaporation and dehydration system top recovered water, bottom extraction treated oil, after the heating unit heating, enter another reaction unit and reacted; 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 1.0-2.0h
-1; The gained reaction product enters high-pressure separation apparatus after heat exchange is cooling.
2. the reforming method with the evaporation and dehydration system producing high-octane gasoline according to claim 1, it 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. the reforming method with the evaporation and dehydration system producing high-octane gasoline according to claim 2, it 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 |
-
2009
- 2009-07-16 CN CN200910088789XA patent/CN102041059B/en active Active
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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