CN201665667U - Prolific arene reforming system capable of simultaneously separating benzene - Google Patents
Prolific arene reforming system capable of simultaneously separating benzene Download PDFInfo
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- CN201665667U CN201665667U CN2009201091854U CN200920109185U CN201665667U CN 201665667 U CN201665667 U CN 201665667U CN 2009201091854 U CN2009201091854 U CN 2009201091854U CN 200920109185 U CN200920109185 U CN 200920109185U CN 201665667 U CN201665667 U CN 201665667U
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 90
- 150000004945 aromatic hydrocarbons Chemical class 0.000 title claims abstract description 26
- 238000002407 reforming Methods 0.000 title claims abstract description 24
- 230000002062 proliferating effect Effects 0.000 title abstract 3
- 238000000605 extraction Methods 0.000 claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 claims abstract description 43
- 238000011084 recovery Methods 0.000 claims abstract description 35
- 230000018044 dehydration Effects 0.000 claims abstract description 27
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 27
- 238000001704 evaporation Methods 0.000 claims abstract description 27
- 230000008020 evaporation Effects 0.000 claims abstract description 27
- 238000010438 heat treatment Methods 0.000 claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000003381 stabilizer Substances 0.000 claims description 13
- 239000002994 raw material Substances 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 2
- 238000007906 compression Methods 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 25
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 25
- 239000001257 hydrogen Substances 0.000 abstract description 25
- 239000007788 liquid Substances 0.000 abstract description 10
- 239000003208 petroleum Substances 0.000 abstract description 3
- 230000006641 stabilisation Effects 0.000 abstract 2
- 238000011105 stabilization Methods 0.000 abstract 2
- 241001120493 Arene Species 0.000 abstract 1
- 238000000034 method Methods 0.000 description 41
- 239000003921 oil Substances 0.000 description 31
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 14
- 239000003054 catalyst Substances 0.000 description 14
- 238000009835 boiling Methods 0.000 description 13
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 12
- 239000000047 product Substances 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 239000005864 Sulphur Substances 0.000 description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 10
- 238000004519 manufacturing process Methods 0.000 description 9
- 239000007795 chemical reaction product Substances 0.000 description 8
- 239000003502 gasoline Substances 0.000 description 8
- 238000010992 reflux Methods 0.000 description 7
- 239000002904 solvent Substances 0.000 description 7
- 238000001833 catalytic reforming Methods 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- 235000019628 coolness Nutrition 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 238000012545 processing Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- 150000001335 aliphatic alkanes Chemical class 0.000 description 4
- 238000003556 assay Methods 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-DYCDLGHISA-N deuterium hydrogen oxide Chemical compound [2H]O XLYOFNOQVPJJNP-DYCDLGHISA-N 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 3
- 239000003209 petroleum derivative Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000004440 column chromatography Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 229910001648 diaspore Inorganic materials 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 229910052702 rhenium Inorganic materials 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000002795 fluorescence method Methods 0.000 description 1
- 239000003269 fluorescent indicator Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009616 inductively coupled plasma Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000003918 potentiometric titration Methods 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- HYERJXDYFLQTGF-UHFFFAOYSA-N rhenium Chemical compound [Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re][Re] HYERJXDYFLQTGF-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000007655 standard test method Methods 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- UWHCKJMYHZGTIT-UHFFFAOYSA-N tetraethylene glycol Chemical compound OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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Abstract
The utility model discloses a prolific arene reforming system capable of simultaneously separating benzene, the system comprises a heating device and a reaction device and is characterized in that the reaction device is connected with a high pressure separator; the high pressure separator is connected with a stabilization tower system; the lower part of the stabilization tower system is connected with an extraction system through a pipeline; on the one hand, the extraction system is connected with an evaporation and dehydration system through the pipeline; on the other hand, the extraction system is connected with a first recovery tower through the pipeline; the upper part of the first recovery tower recovers the benzene through the pipeline, and the lower part is connected with a second recovery tower through the pipeline; the upper part of the second recovery tower recovers mixed arenes through the pipeline, and the lower part is connected with the extraction system through the pipeline; the bottom part of the evaporation and dehydration system is connected with the other reaction device through the pipeline and the heating device, and the top part of the evaporation and dehydration system directly recovers water through the pipeline; and the other end of the other reaction device is connected with the high pressure separator through the pipeline. The petroleum naphtha prolific arene reforming system has the advantages of greatly improving the treatment capacity, the liquid yield, the arene productivity and the hydrogen output.
Description
Technical field
The utility model relates to a kind of reforming system, and particularly a kind of productive aromatic hydrocarbon is isolated the reforming system of benzene 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 the naphtha productive aromatic hydrocarbon reforming system of raising liquid yield, aromatic production, octane value and hydrogen output just becomes the difficult problem that this technical field is badly in need of solution.
Summary of the invention
The purpose of this utility model provides and a kind ofly can improve processing power, and improves the naphtha productive aromatic hydrocarbon reforming system that liquid yield, aromatic production and hydrogen yield provide the high-octane rating product simultaneously.
For achieving the above object, the utility model is taked following technical scheme:
A kind of productive aromatic hydrocarbon is isolated the reforming system of benzene simultaneously, comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit is divided into two portions, first and/or second reaction unit (and/or more reaction units) is connected with evaporation and dehydration system by high-pressure separator, stabilizer tower system and extraction system, described extraction system links to each other with second recovery column by first recovery column again, and described second recovery column bottom is connected with described extraction system by pipeline; 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 productive aromatic hydrocarbon is isolated the reforming system of benzene simultaneously, comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit bottom is connected with high-pressure separator by pipeline; Described high-pressure separator is connected with the stabilizer tower system by pipeline, and is connected with the raw material supply system by pipeline and compression set; Described stabilizer tower system bottom is connected with extraction system by pipeline; Described extraction system is connected with evaporation and dehydration system by pipeline on the one hand; Described extraction system is connected with first recovery column by pipeline on the other hand; Described first recovery column top is by pipeline extraction benzene, and described first recovery column bottom 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; Described evaporation and dehydration system top is by the pipeline recovered water, described evaporation and dehydration system bottom is connected with another reaction unit (the 3rd reaction unit) by pipeline and heating unit, and the other end of described another reaction unit is connected with described high-pressure separator with refrigerating unit by pipeline.
A kind of optimal technical scheme, it is characterized in that: described reaction unit is connected with second reaction unit (can link to each other with more reaction unit by heating unit behind second reaction unit) by second heating unit earlier again, and then is connected with described high-pressure separator.
A kind of optimal technical scheme, it is characterized in that: described another reaction unit is connected with the 4th reaction unit (can link to each other with more reaction unit again by heating unit behind the 4th reaction unit) by the 4th heating unit earlier, and then is connected with described high-pressure separator.
A kind of optimal technical scheme is characterized in that: described reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
A kind of optimal technical scheme is characterized in that: described another reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
Extraction system described in the utility model is that the patent No. is a disclosed extraction system in 200310103541.9 and 200310103540.4, comprises solvent recuperation, water wash system, returns the system of washing etc.
System of stabilizer tower described in the utility model and evaporation and dehydration system are conventional system, comprise tower, air-cooler, watercooler, return tank, reflux pump and column bottoms pump etc.
Process furnace described in the utility model and condensing works are conventional device.
Catalyst system therefor described in the utility model in the reactor is conventional reforming catalyst.
Beneficial effect:
The advantage that productive aromatic hydrocarbon of the present utility model is isolated the reforming system of benzene simultaneously is: compare with existing catalytic reforming process, productive aromatic hydrocarbon of the present utility model is isolated in the reforming system of benzene simultaneously, under than low reaction pressure reacted product through extracting and dehydration by evaporation after, the treated oil that generates with enter another reactor after recycle hydrogen mixes and further react, make the processing power of system of the present utility model improve, liquid yield, aromatic production and hydrogen yield improve greatly, the high-octane rating product is provided simultaneously, owing to isolated benzene, make the benzene content of premium blend component BTX aromatics reduce greatly in addition.
Below by the drawings and specific embodiments the utility model is described further, but and does not mean that restriction the utility model protection domain.
Description of drawings
Fig. 1 is the schematic flow sheet of the utility model embodiment 1.
Fig. 2 is the schematic flow sheet of the utility model embodiment 2.
Fig. 3 is the schematic flow sheet of the utility model embodiment 3.
Embodiment
Embodiment 1
As shown in Figure 1, be the schematic flow sheet of the utility model embodiment 1.With boiling range is 80-185 ℃, and sulphur content is 0.5ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 70% (m), and naphthene content is 28% (m), aromaticity content is 2% (m), and octane value (RON) is that 42,20 ℃ of density are 732 kilograms/meter
3, flow is the process heat exchange earlier of the refining feed naphtha (a) of 12.5 tons/hour paraffinic base, through after the process furnace 1-1 heating, enters reactor 2-1 and reacts again, the feed volume air speed is 3.0h
-1The temperature in of described reactor 2-1 is 530 ℃, and inlet pressure is 1.0MPa (absolute pressure); The gained reaction product enters reactor 2-2 and reacts after heating through process furnace 1-2, and the temperature in of described reactor 2-2 is 530 ℃, and inlet pressure is 1.0MPa (absolute pressure); Reaction product enters high-pressure separator 4 and carries out the high pressure separation after heat exchange and condenser 3 coolings, the service temperature of described high-pressure separator 4 is 35 ℃, and working pressure is 1.2MPa (absolute pressure); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.613 ton/hour, and pure hydrogen flow is 0.455 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 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 2.401 tons/hour; Gained reformed oil at the bottom of the tower (boiling range is 35-196 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 100 ℃, and working pressure is 0.6MPa (absolute pressure), and solvent ratio is 3.0, returns and washes than being 0.5, and solvent for use is a tetramethylene sulfone; After extraction system 8 extractings, gained is extracted oil out and is entered the middle part of first recovery column 9-1 by bottom and pipeline, and the tower top temperature of described first recovery column 9-1 is 85 ℃, and pressure is 0.1MPa (absolute pressure), column bottom temperature is 175 ℃, and pressure is 0.15MPa (absolute pressure); Top extraction benzene (f), the purity of gained benzene are 99.99%, and freezing point is 5.45 ℃, and 20 ℃ of density are 879 kilograms/meter
3, flow is 0.274 ton/hour; The bottom production enters second recovery column 9-2, and the service temperature of described second recovery column 9-2 is 110 ℃, and working pressure is 0.02MPa (absolute pressure); Top extraction BTX aromatics (e), the gained BTX aromatics can be used as gasoline and is in harmonious proportion product or directly as aromatic hydrocarbon product, its boiling range is 80-196 ℃, sulphur content trace (can not detecting), non-aromatics content is 2.0% (m), and aromaticity content is 98.0% (m), and benzene content is 0.33% (m), octane value (RON) is that 129,20 ℃ of density are 861 kilograms/meter
3, flow is 9.211 tons/hour, and aromatics yield is 74.40% (weight), and total liquid yield is 75.88%; The bottom production returns the top that enters extraction system 8; After extraction system 8 extractings, the gained dehydration by evaporation tower 7 (other does not draw) that top through extraction system 8 enters in the evaporation and dehydration system of raffinating oil dewaters, the head temperature of the dehydration by evaporation tower 7 in the described evaporation and dehydration system is 110 ℃, pressure is 0.4MPa (absolute pressure), bottom temp is 210 ℃, pressure is 0.45MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; Extraction treated oil in bottom is as the charging of reactor 2-3, and the boiling range of gained treated oil is 35-186 ℃, sulphur content trace (can not detecting), non-aromatics content is 98.8% (m), aromaticity content is 1.2% (m), and octane value (RON) is that 63,20 ℃ of density are 738 kilograms/meter
3, flow is 4.837 tons/hour; Enter reactor 2-3 after the gained treated oil heats through process furnace 1-3 and react, the temperature in of described reactor 2-3 is 530 ℃, and inlet pressure is 1.0MPa (absolute pressure); The gained reaction product enters reactor 2-4 reaction after process furnace 1-4 heating, the temperature in of described reactor 2-4 is 530 ℃, and inlet pressure is 1.0MPa (absolute pressure), and the feed volume air speed is 1.0h
-1The gained reaction product with after the reaction product of described reactor 2-2 is mixed through entering high-pressure separator 4 after heat exchange and condenser 3 coolings.
Wherein pack into the ratio of catalytic amount of each reactor is:
Reactor 2-1: reactor 2-2=1: 1.5; Reactor 2-3: reactor 2-4=1: 2.
The used reforming catalyst of the utility model is a kind of Pt, Re reforming catalyst, its carrier mixes by a certain percentage for single diaspore of GM and the single diaspore of Ziegler synthesising by-product SB that adopts aluminium colloidal sol deep fat ageing process and make, the compound γ-aluminium sesquioxide that two concentrated Kong Feng are arranged that makes through moulding, roasting.Pt content is 0.10～1.00 heavy % on the catalyzer, and Re content is 0.10～3.00 heavy %, and Cl content is 0.50～3.00 heavy %, and this catalyzer has the characteristics of high reactivity, highly selective and low carbon deposit.
Total liquid yield equals the flow sum of BTX aromatics and benzene divided by the raw material inlet amount in the utility model.
Aromatics yield equals the BTX aromatics flow and multiply by aromaticity content and add that the flow of benzene is again divided by the raw material inlet amount.
Hydrogen yield equals to efflux the hydrogen amount and multiply by hydrogen purity again divided by the raw material inlet amount.
The physico-chemical property of reactor 2-1 and 2-2 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g? | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％? | Re m％? |
| 192? | 183? | 0.52? | 0.75? | 0.25? | 0.25? |
The physico-chemical property of reactor 2-3 and 2-4 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g? | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％? | Re m％? |
| 196? | 187? | 0.54? | 0.74? | 0.26? | 0.45? |
The used measuring method of the utility model is (down together):
1, boiling range: GB/T6536-1997 measured for petroleum product distillation method;
2, sulphur content: the total sulfur content assay method (ultraviolet fluorescence method) of SH/T0689-2000 light hydrocarbon and motor spirit and other oil products;
3, mercaptan sulfur: mercaptan sulfur assay method (potentiometric titration) in the GB/T1792-1988 distillate fuel oil;
4, alkane: SH/T0239-92 thin layer packed column chromatography;
5, aromatic hydrocarbons: GB/T11132-2002 liquid petroleum product hydro carbons assay method (fluorescent indicator adsorption method);
6, octane value: GB/T5487 testing octane number of gasoline method (organon);
7, density: GB/T1884-2000 crude oil and liquid petroleum product density experiment chamber assay method (densimeter method);
8, naphthenic hydrocarbon: SH/T0239-92 thin layer packed column chromatography;
9, metal in the oil: the standard test methods of nickel, vanadium and iron in ASTM D 5708-2005 inductively coupled plasma (ICP) aes determination crude oil and the trapped fuel;
10, nitrogen content: the SH/T0704-2001 chemoluminescence method is surveyed nitrogen (boat sample introduction).
Embodiment 2
As shown in Figure 2, be the schematic flow sheet of the utility model embodiment 2.With boiling range is 80-185 ℃, and sulphur content is 0.54ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 60% (m), and naphthene content is 34% (m), aromaticity content is 6% (m), and octane value (RON) is that 50,20 ℃ of density are 738 kilograms/meter
3, flow is the process heat exchange earlier of the refining feed naphtha (a) of 12.5 tons/hour intermediate base, through after the process furnace 1-1 heating, enters reactor 2-1 and reacts again; The feed volume air speed is 4.0h
-1Wherein said reactor 2-1 is gone up by reactor 2-1 and following two reactors in series of reactor 2-1 are formed, and is connected with process furnace 1-2 by pipeline therebetween; Described reactor 2-1 go up and reactor 2-1 under temperature in 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 0.474 ton/hour, and pure hydrogen flow is 0.428 ton/hour, and hydrogen yield is 3.42% (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 1.0MPa (absolute pressure), and reflux ratio (m/m) is 0.99; Cat head extraction dry gas, liquefied gas and less water (c), its flow is 1.448 tons/hour; Gained reformed oil at the bottom of the tower (boiling range is 35-194 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 120 ℃, and working pressure is 0.8MPa (absolute pressure), and solvent ratio is 5, returns and washes than being 0.7, and solvent for use is the N-formyl morpholine; Through after the extracting, the gained extraction system is extracted oil out and is entered first recovery column 9-1, and the tower top temperature of described first recovery column is 87 ℃, and pressure is 0.15MPa (absolute pressure), and column bottom temperature is 175 ℃, and pressure is 0.2MPa (absolute pressure); Top extraction benzene (f), the purity of gained benzene are 99.99%, and freezing point is 5.45 ℃, and 20 ℃ of density are 879 kilograms/meter
3, flow is 0.454 ton/hour; The bottom production enters second recovery column 9-2, and the service temperature of described second recovery column is 130 ℃, and working pressure is 0.035MPa (absolute pressure); Top extraction BTX aromatics (e), the gained BTX aromatics can be used as gasoline and is in harmonious proportion product or directly as aromatic hydrocarbon product, its boiling range is 80-194 ℃, sulphur content trace (can not detecting), non-aromatics content is 1.9% (m), and aromaticity content is 98.1% (m), and benzene content is 0.49% (m), octane value (RON) is that 131,20 ℃ of density are 862 kilograms/meter
3, flow is 10.123 tons/hour, and aromatics yield is 83.08% (weight), and total liquid yield is 84.62% (weight); The bottom production returns and enters extraction system; After extraction system 8 extractings, the gained dehydration by evaporation tower 7 (other does not draw) that top through extraction system 8 enters in the evaporation and dehydration system of raffinating oil dewaters, the head temperature of the dehydration by evaporation tower 7 in the described evaporation and dehydration system is 120 ℃, pressure is 0.5MPa (absolute pressure), bottom temp is 225 ℃, pressure is 0.55MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; Bottom extraction treated oil (as the charging of the second reactor 2-2), the boiling range of gained treated oil is 35-184 ℃, sulphur content trace (can not detecting), non-aromatics content is 98.7% (m), aromaticity content is 1.3% (m), and octane value (RON) is that 63,20 ℃ of density are 740 kilograms/meter
3, flow is 5.076 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 be connected with process furnace 1-4 by pipeline; Described reactor 2-2 go up and reactor 2-2 under temperature in be 500 ℃, inlet pressure is 1.3MPa (absolute pressure), the feed volume air speed is 1.5h
-1Enter high-pressure separator 4 after process heat exchange of gained reaction product and condenser 3 coolings.
Wherein pack into the ratio of catalytic amount of each reactor is:
On the reactor 2-1: under the reactor 2-1=1: 2;
On the reactor 2-2: under the reactor 2-2=1: 2.5.
The physico-chemical property of reactor 2-1 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g? | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％? | Re m％? |
| 192? | 183? | 0.52? | 0.75? | 0.25? | 0.25? |
The physico-chemical property of reactor 2-2 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g? | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％? | Re m％? |
| 196? | 187? | 0.54? | 0.74? | 0.26? | 0.45? |
Embodiment 3
As shown in Figure 3, be the schematic flow sheet of the utility model embodiment 3.With boiling range is 80-185 ℃, and sulphur content is 0.45ppm, and nitrogen content 0.5ppm, metal content are 5ppb, water content 5ppm, alkane content are 47% (m), and naphthene content is 42% (m), aromaticity content is 11% (m), and octane value (RON) is that 61,20 ℃ of density are 742 kilograms/meter
3, flow is the process heat exchange earlier of the refining petroleum naphtha (a) of 12.5 tons/hour cycloalkyl, through after the process furnace 1-1 heating, enters reactor 2-1 and reacts again; The feed volume air speed is 5.0h
-1The temperature in of described reactor 2-1 is 470 ℃, and inlet pressure is 1.6MPa (absolute pressure); The gained reaction product enters high-pressure separator 4 and carries out the high pressure separation after heat exchange and condenser 3 coolings, the service temperature of described high-pressure separator 4 is 45 ℃, and working pressure is 1.4MPa (absolute pressure); After the high pressure separation, a gained hydrogen part is sent (b) outside, and its flow is 0.419 ton/hour, and pure hydrogen flow is 0.382 ton/hour, and hydrogen yield is 3.06% (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 1.565 tons/hour; Gained reformed oil at the bottom of the tower (boiling range is 35-192 ℃) enters extraction system 8 and handles, and the service temperature of described extraction system 8 is 150 ℃, and working pressure is 1.0MPa (absolute pressure), and solvent ratio is 8.0, returns and washes than being 1.0, and solvent for use is a Tetraglycol 99; After extraction system 8 extractings, gained is extracted oil enters first recovery column 9-1 from the bottom of extraction system 8 middle part out, and the tower top temperature of described first recovery column 9-1 is 90 ℃, and pressure is 0.2MPa (absolute pressure), column bottom temperature is 175 ℃, and pressure is 0.25MPa (absolute pressure); Top extraction benzene (f), the purity of gained benzene are 99.99%, and freezing point is 5.45 ℃, and 20 ℃ of density are 879 kilograms/meter
3, flow is 0.335 ton/hour; The bottom production enters the middle part of second recovery column 9-2, and the service temperature of described second recovery column 9-2 is 155 ℃, and working pressure is 0.05MPa (absolute pressure); Top extraction BTX aromatics (e), the gained BTX aromatics can be used as gasoline and is in harmonious proportion product or directly as aromatic hydrocarbon product, its boiling range is 80-192 ℃, sulphur content trace (can not detecting), non-aromatics content is 1.8% (m), and aromaticity content is 98.2% (m), and benzene content is 0.36% (m), octane value (RON) is that 134,20 ℃ of density are 865 kilograms/meter
3, flow is 10.298 tons/hour, and aromatics yield is 83.52% (weight), and total liquid yield is 85.06% (weight); The bottom production of described second recovery column 9-2 returns and enters extraction system 8; After extraction system 8 extractings, the gained dehydration by evaporation tower 7 that top through extraction system 8 enters in the evaporation and dehydration system of raffinating oil dewaters, the head temperature of the dehydration by evaporation tower 7 in the described evaporation and dehydration system is 130 ℃, pressure is 0.6MPa (absolute pressure), bottom temp is 240 ℃, pressure is 0.65MPa (absolute pressure), total reflux; Top extraction less water (d), its flow are 0.001 ton/hour; Bottom extraction treated oil (as the charging of reactor 2-2), the boiling range of gained treated oil is 35-182 ℃, sulphur content trace (can not detecting), non-aromatics content is 1.5% (m), aromaticity content is 98.5% (m), and octane value (RON) is 64, is 745 kilograms/meter 20 ℃ of density
3, flow is 4.614 tons/hour; Enter reactor 2-2 after described treated oil heats through process furnace 1-2 and react, the temperature in of described reactor 2-2 is 470 ℃, and inlet pressure is 1.6MPa (absolute pressure), and the feed volume air speed is 2.0h
-1Enter high-pressure separator 4 after process heat exchange of gained reaction product and condenser 3 coolings.
Wherein pack into the ratio of catalytic amount of each reactor is:
Reactor 2-1: reactor 2-2=1: 2.
The physico-chemical property of reactor 2-1 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g? | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％? | Re m％? |
| 192? | 183? | 0.52? | 0.75? | 0.25? | 0.25? |
The physico-chemical property of reactor 2-2 catalyst system therefor is as shown in the table:
| Specific surface area m 2/g? | Intensity N/cm | Pore volume ml/g | Bulk density g/ml | Pt m％? | Re m％? |
| 196? | 187? | 0.54? | 0.74? | 0.26? | 0.45? |
Claims (6)
1. a productive aromatic hydrocarbon is isolated the reforming system of benzene simultaneously, comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit is divided into two portions, first and/or second reaction unit is connected with evaporation and dehydration system by high-pressure separator, stabilizer tower system and extraction system, described extraction system links to each other with second recovery column by first recovery column again, and described second recovery column bottom is connected with described extraction system by pipeline; Described evaporation and dehydration system is connected with the 3rd and/or the 4th reaction unit again.
2. a productive aromatic hydrocarbon is isolated the reforming system of benzene simultaneously, comprises heating unit, the reaction unit that is attached thereto; It is characterized in that: described reaction unit bottom is connected with high-pressure separator by pipeline; Described high-pressure separator is connected with the stabilizer tower system by pipeline, and is connected with the raw material supply system by pipeline and compression set; Described stabilizer tower system bottom is connected with extraction system by pipeline; Described extraction system is connected with evaporation and dehydration system by pipeline on the one hand; Described extraction system is connected with first recovery column by pipeline on the other hand; Described first recovery column top is by pipeline extraction benzene, and described first recovery column bottom 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; Described evaporation and dehydration system top is by the pipeline recovered water, described evaporation and dehydration system bottom is connected with another reaction unit by pipeline and heating unit, and the other end of described another reaction unit is connected with described high-pressure separator with refrigerating unit by pipeline.
3. productive aromatic hydrocarbon according to claim 2 is isolated the reforming system of benzene simultaneously, it 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. productive aromatic hydrocarbon according to claim 3 is isolated the reforming system of benzene simultaneously, it is characterized in that: described another reaction unit is connected with the 4th reaction unit by the 4th heating unit earlier, and then is connected with described high-pressure separator.
5. productive aromatic hydrocarbon according to claim 2 is isolated the reforming system of benzene simultaneously, it is characterized in that: described reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
6. productive aromatic hydrocarbon according to claim 5 is isolated the reforming system of benzene simultaneously, it is characterized in that: described another reaction unit is placed in-line two reactors up and down, is connected by heating unit therebetween.
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| CN2009201091854U CN201665667U (en) | 2009-06-17 | 2009-06-17 | Prolific arene reforming system capable of simultaneously separating benzene |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101921619A (en) * | 2009-06-17 | 2010-12-22 | 北京金伟晖工程技术有限公司 | Reforming system and method for fecundating aromatic hydrocarbons and simultaneously isolating benzene |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101921619A (en) * | 2009-06-17 | 2010-12-22 | 北京金伟晖工程技术有限公司 | Reforming system and method for fecundating aromatic hydrocarbons and simultaneously isolating benzene |
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