CN1752182A - Method for producing aromatic hydrocarbon rubber filling oil - Google Patents
Method for producing aromatic hydrocarbon rubber filling oil Download PDFInfo
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- CN1752182A CN1752182A CN 200510018058 CN200510018058A CN1752182A CN 1752182 A CN1752182 A CN 1752182A CN 200510018058 CN200510018058 CN 200510018058 CN 200510018058 A CN200510018058 A CN 200510018058A CN 1752182 A CN1752182 A CN 1752182A
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Abstract
A process for preparing the arylhydrocarbon-type filling oil for rubber includes such steps as mixing tar fraction with H2, hydrogenating reaction on hydromodifying catalyst Mo-Ni-P for removing S, N, colloid and asphalt from tar fraction, separating out H2, dry gas, H2S, NH4 and liquefied gas to obtain liquid, fractionating, and cutting.
Description
Technical field
The invention belongs to coal chemical technology, relate to a kind of production method of aromatic hydrocarbon rubber filling oil.
Background technology
Rubber filling oil is a kind of special type oil that is used to produce oil-extended rubber.After rubber was oil-filled, processing characteristics and use properties can both improve, and had increased rubber output simultaneously, had reduced cost.The output of China's natural rubber is limited, and synthetic rubber occupies very big ratio in rubber industry.Along with the raising of China's synthetic rubber development of technology, output, the output of oil-extended rubber is also increasing sharply, so the demand of rubber filling oil also grows with each passing day; Wherein, good, the oil-filled amount of aromatic hydrocarbon rubber filling oil and all kinds of rubber compatibility is big, so consumption is also maximum.
At present, domestic only indivedual petroleum refinery utilizes straight run to extract oil out directly as aromatic hydrocarbon rubber filling oil, limited amount, quality is also very unstable, be difficult to satisfy the different requirements of different rubber plants, influenced the production of oil-extended rubber, cause some rubber production factories to need import extending oil.CN1022844C discloses a kind of method of utilizing wax oil to produce high-value product, adopts solvent extraction and other technical optimization to make up faulty wax oil is processed and produced aromatic hydrocarbon rubber filling oil.The disclosed a kind of method of CN87105674A is that clarified oil that the heavy distillate of catalytic cracking is obtained after through sedimentation, clarification, filtration is as aromatic hydrocarbon rubber filling oil.Although these method Technology maturations, Production Flow Chart are simple, output is limited, is difficult for the formation scale.Simultaneously, because the continuous minimizing of petroleum resources, in order sufficiently and reasonably to utilize petroleum resources, each factory of great oil refining all the problem of heavy oil lighting as research, produces light Fuel to greatest extent, to improve the throughput of refinery.Therefore, utilizing the part heavy oil of refinery by-product to produce aromatic hydrocarbon rubber filling oil far can not meet the need of market.So, seek new raw material sources and be of great practical significance to produce qualified aromatic hydrocarbon rubber filling oil.
China is a country that coal resource is very abundant, and the coal tar of Coal Chemical Industry process by-product has the characteristic of natural crude oil, and how effectively utilizing coal tar is the important step of the comprehensive utilization of coal.Usual method is to produce Chemicals such as benzene, pyridine with the chemical industry method, but this method is separated or the purification difficulty is bigger, is difficult for the formation scale; Have coal tar is used as oil fuel after overpickling, alkali cleaning, but acid sludge, alkaline residue that this method produces are difficult to processing, seriously polluted, oil fuel does not meet environmental protection standard yet yet.Therefore, it is most important sufficiently and reasonably to utilize abundant coal tar fraction to produce high-value product.
Summary of the invention
Technical problem to be solved by this invention is: existingly utilize the existing insufficient raw material of method, the output of refinery products and co-production aromatic hydrocarbon rubber filling oil limited, the problem of unstable product quality.
For addressing the above problem, the technical solution used in the present invention is: a kind of production method of aromatic hydrocarbon rubber filling oil is characterized in that being made up of following steps:
A. coal tar fraction and hydrogen enter hydrogenator after mixing, with Mo-Ni-P catalyst for hydro-upgrading contact reacts, remove sulphur, nitrogen impurity and colloid, bituminous matter in the coal tar fraction, reaction conditions is: hydrogen dividing potential drop 8.0～14.0MPa, 370～390 ℃ of temperature of reaction, volume space velocity 0.6～1.0h
-1, hydrogen to oil volume ratio 1000～1200, reaction afterreaction product is derived hydrogenator;
Described Mo-Ni-P catalyst for hydro-upgrading, in oxide dry basis, MoO
3Account for 15～25w% of total catalyst weight, NiO accounts for 2～6w% of total catalyst weight, P
2O
5Account for 3～8w% of total catalyst weight, all the other are the amorphous silicic acid alumina supporter;
B. the reaction product that obtains of steps A enters gas delivery and stable system after heat exchange, cooling, isolate hydrogen, dry gas, hydrogen sulfide and ammonia and liquefied gas after, obtain product liquid;
C. the product liquid that step B is obtained carries out fractionation, cutting in separation column, obtains cut more than 360 ℃, and this cut is the aromatic hydrocarbon rubber filling oil product.
Adopt the present invention, have following beneficial effect: (1) the present invention utilizes fixed bed hydrogenation device and technical process conventional in the refining of petroleum industry, the Technology maturation, and Production Flow Chart is simple; (2) the present invention does not have special requirement to raw material, can make full use of the coal tar fraction that industrial dry distillation of coal device is produced, and raw material sources are wide, and processing power is big; (3) aromatic hydrocarbon rubber filling oil that adopts the inventive method to produce, its sulphur content is lower than 500 μ g/g, and nitrogen content is lower than 1000 μ g/g, and aromaticity content is not less than 90w% (w% represents weight percentage); Good security, and nontoxic, free from extraneous odour have no adverse effects to environment; (4) constantly increase and under the situation that oil supply day is becoming tight, the present invention has opened up new raw material sources for producing aromatic hydrocarbon rubber filling oil in the aromatic hydrocarbon rubber filling oil demand.The inventive method is suitable for producing on a large scale aromatic hydrocarbon rubber filling oil, can solve the underproduce problem of aromatic hydrocarbon rubber filling oil.In addition, utilizing the coal tar fraction hydro-upgrading to produce qualified aromatic hydrocarbon rubber filling oil is a brand-new thinking, does not see the report of relevant this respect up to now as yet; Thus, the present invention provides new approach for the comprehensive utilization of coal tar again.
The present invention is further detailed explanation below in conjunction with embodiment and embodiment.Embodiment and embodiment do not limit the scope of protection of present invention.
Embodiment
The production method of aromatic hydrocarbon rubber filling oil of the present invention, form by following steps:
A. coal tar fraction and hydrogen enter hydrogenator after mixing, and with Mo-Ni-P catalyst for hydro-upgrading contact reacts, remove sulphur, nitrogen impurity and colloid, bituminous matter in the coal tar fraction.Coal tar fraction is meant the coal tar after isolating phenol, naphthalene and tar-bitumen on the existing industrial dry distillation of coal device of Coal Chemical Industry industry, its sulphur content is generally 0.3～1.0w%, nitrogen content is generally 0.4～1.2w%, initial boiling point generally is not less than 150 ℃, do and generally be no more than 530 ℃, aromaticity content is generally 75～90w%, and colloid and asphalt content are generally 5～15w%.Hydrogenator adopts conventional fixed bed hydrogenation reactor, and the operating method that adopts one way to pass through.After coal tar fraction and hydrogen are mixed, generally be preheating to through interchanger, process furnace that the top from hydrogenator enters hydrogenator after 330～350 ℃, in hydrogenator and flow to current downflow.Coal tar fraction and the hydrogen reaction conditions in hydrogenator is: hydrogen dividing potential drop 8.0～14.0MPa, 370～390 ℃ of temperature of reaction, volume space velocity 0.6～1.0h-1, hydrogen to oil volume ratio 1000～1200.Reaction afterreaction product is derived hydrogenator from the bottom of hydrogenator.
Described Mo-Ni-P catalyst for hydro-upgrading is for being supported on the Mo-Ni-P catalyst for hydro-upgrading on the amorphous silicic acid alumina supporter; In oxide dry basis, MoO
3Account for 15～25w% of total catalyst weight, NiO accounts for 2～6w% of total catalyst weight, P
2O
5Account for 3～8w% of total catalyst weight, all the other are the amorphous silicic acid alumina supporter.The pore volume of catalyzer is generally 0.3～0.5ml/g, and specific surface is generally 330～400m
2/ g; Be shaped as sphere, diameter is generally φ 1.5～3mm.This catalyzer has stronger desulfurization, denitrogenation ability, and can remove colloid and bituminous matter in the coal tar fraction.This catalyzer system adopts catalyst for hydro-upgrading preparation method preparation conventional in the refining of petroleum industry.
B. the reaction product that obtains of steps A enters gas delivery and stable system after heat exchange, cooling, isolate hydrogen, dry gas, hydrogen sulfide and ammonia and liquefied gas after, obtain product liquid.Wherein, gas delivery and stable system comprise high-pressure separator, light pressure separator and the stabilizer tower that links to each other successively.The reaction product that steps A obtains through heat exchange, enter high-pressure separator after being cooled to normal temperature (30～50 ℃), is isolated most hydrogen, most of dry gas (C in heat exchange, cooling apparatus
1～C
2Component), most of hydrogen sulfide and ammonia, a small amount of liquefied gas (C
3～C
4Component), enter light pressure separator then; In light pressure separator, isolate remaining most of liquefied gas, most of hydrogen sulfide and ammonia, remaining hydrogen and dry gas, enter stabilizer tower afterwards; In stabilizer tower, isolate remaining liquefied gas, hydrogen sulfide and ammonia.In the said process, the hydrogen-rich gas that high-pressure separator is isolated have been removed behind most of hydrogen sulfide and the ammonia impurity recycles.Above-mentioned gas delivery and stable system and operating process thereof, operational condition all are conventional, identical with in the conventional fixed bed hydrogenation device of refining of petroleum.
C. the product liquid that step B is obtained (C5 and above component are flowed out by stabilizer tower) carries out fractionation, cutting in separation column, isolates 360 ℃ and following cut, obtains cut more than 360 ℃, sends into the product jar.This more than 360 ℃ cut be the aromatic hydrocarbon rubber filling oil product.Above-mentioned cut more than 360 ℃, be meant product liquid more than 360 ℃ to the cut of its final boiling point.Described separation column is an atmospheric fractional tower, and its operational condition adopts the routine operation condition.
The aromatic hydrocarbon rubber filling oil that the invention described above processing method is produced, its sulphur content are lower than 500 μ g/g, and nitrogen content is lower than 1000 μ g/g, and aromaticity content is not less than 90w%, and colloid and asphalt content are not higher than 2w%; Initial boiling point is higher than 360 ℃, does to be no more than 550 ℃; Good security, and nontoxic, free from extraneous odour have no adverse effects to environment.
Embodiment
Embodiment 1
On small test device, test.The hydrogenator of this device is the 100ml fixed bed hydrogenation reactor, and separation column is the true boiling point distillation device with 17 blocks of theoretical trays.The coal tar (having isolated phenol, naphthalene and tar-bitumen) that the coal tar fraction that test is processed is produced for certain industrial dry distillation of coal device, its main character is referring to table 1.Filling is supported on the Mo-Ni-P catalyst for hydro-upgrading on the amorphous silicic acid alumina supporter, its MoO in the 100ml fixed bed hydrogenation reactor
3Content is 22.8w%, and NiO content is 3.4w%, P
2O
5Content is 4.8w%, and all the other are the amorphous silicic acid alumina supporter.The pore volume of catalyzer is that 0.38ml/g, specific surface are 363m
2/ g is shaped as sphere, and diameter is φ 2.0mm.This catalyzer adopts conventional pre-vulcanization process to carry out prevulcanized before use, treat that catalyst activity is stable after, carry out processing condition again and investigate test (following examples are herewith).
At embodiment 1 (and among following embodiment 2 and embodiment 3), the gas delivery of testing apparatus and stable system only are provided with high-pressure separator, and light pressure separator and stabilizer tower are not set.
In the operating process, the top from hydrogenator after above-mentioned coal tar fraction and hydrogen mix enters hydrogenator, with Mo-Ni-P catalyst for hydro-upgrading contact reacts.The operating method that test adopts one way to pass through is carried out hydro-upgrading to coal tar fraction.Reaction afterreaction product is derived from the bottom of hydrogenator, enters high-pressure separator after being cooled to normal temperature, in high-pressure separator most of hydrogen, dry gas, hydrogen sulfide and ammonia and a spot of liquefied gas is separated.Enter surge tank afterwards, under the routine operation condition, carry out gas and carry, remaining liquefied gas and remaining hydrogen, dry gas, hydrogen sulfide and ammonia are separated with nitrogen.Isolate the product liquid (C that obtains behind the above-mentioned gas
5And above component) flows out by surge tank, send into the true boiling point distillation device and carry out fractionation.In the true boiling point distillation device, cut out 360 ℃ and following lighting end, obtain cut more than 360 ℃; This more than 360 ℃ cut be aromatic hydrocarbon rubber filling oil product of the present invention.
In the above-mentioned sepn process, the isolated hydrogen-rich gas of high-pressure separator does not recycle.
Among the embodiment 1, hydrogenation modifying process condition (being the reaction conditions of hydrogenator) and cut more than 360 ℃ (refer to more than 360 ℃ to the cut of final boiling point aromatic hydrocarbon rubber filling oil promptly of the present invention; Following examples are herewith) product property referring to table 2.In order to investigate contrast, listed the aromatic hydrocarbon rubber filling oil company standard of Sinopec Group's formulation, execution in the table 2 in the lump.As can be seen from Table 2, the sulphur content of embodiment 1 resulting aromatic hydrocarbon rubber filling oil is 368 μ g/g, and nitrogen content is 826 μ g/g, and aromaticity content is 94.1w%, and colloid and asphalt content are 1.7w%; Good security, and nontoxic, free from extraneous odour have no adverse effects to human body and environment.
Embodiment 2
Press embodiment 1, different is the component concentration and the physical parameter of hydrogenation modifying process condition and Mo-Ni-P catalyst for hydro-upgrading.The hydrogenation modifying process condition and more than 360 ℃ the product property of cut referring to table 2.The MoO of used Mo-Ni-P catalyst for hydro-upgrading
3Content is 20.5w%, and NiO content is 4.6w%, P
2O
5Content is 5.9w%, and all the other are the amorphous silicic acid alumina supporter.The pore volume of catalyzer is that 0.40ml/g, specific surface are 375m
2/ g is shaped as sphere, and diameter is φ 2.5mm.
Testing apparatus, coal tar fraction, procedure of processing and other unaccounted operating process that embodiment 2 is used, all identical with embodiment 1.
As can be seen from Table 2, the sulphur content of embodiment 2 resulting aromatic hydrocarbon rubber filling oils is 352 μ g/g, and nitrogen content is 786 μ g/g, and aromaticity content is 93.5w%, and colloid and asphalt content are 1.5w%; Good security, and free from extraneous odour are a kind of environment amenable products.
Embodiment 3
Press embodiment 1, different is the component concentration and the physical parameter of hydrogenation modifying process condition and Mo-Ni-P catalyst for hydro-upgrading.The hydrogenation modifying process condition and more than 360 ℃ the product property of cut referring to table 2.The MoO of used Mo-Ni-P catalyst for hydro-upgrading
3Content is 18.1w%, and NiO content is 5.4w%, P
2O
5Content is 6.8w%, and all the other are the amorphous silicic acid alumina supporter.The pore volume of catalyzer is that 0.42ml/g, specific surface are 388m
2/ g is shaped as sphere, and diameter is φ 2.8mm.
Testing apparatus, coal tar fraction, procedure of processing and other unaccounted operating process that embodiment 3 is used, all identical with embodiment 1.
As can be seen from Table 2, the sulphur content of embodiment 3 resulting aromatic hydrocarbon rubber filling oils is 375 μ g/g, and nitrogen content is 844 μ g/g, and aromaticity content is 94.8w%, and colloid and asphalt content are 1.8w%; Good product quality, and nontoxic, free from extraneous odour have the characteristics of environmentally friendly machine.
The main character of table 1 coal tar fraction
(embodiment 1～embodiment 3)
| Project | |
| Density, 20 ℃, kg/m 3 | 1135.2 |
| Carbon residue, w% | 1.41 |
| Pour point, ℃ | 1 |
| Viscosity, 100 ℃, mm 2/s | 3.926 |
| Sulphur content, μ g/g | 7147 |
| Nitrogen content, μ g/g | 9036 |
| Aromaticity content, w% | 82.1 |
| Colloid and asphalt content, w% | 9.3 |
| Boiling range (D2887), ℃ | |
| IBP/10％ | 154/242 |
| 50％/90％ | 340/429 |
| 95％/FBP | 464/513 |
| Smell | Pungent odour |
The table 2 hydrogenation modifying process condition and the product property of cut more than 360 ℃
(embodiment 1～embodiment 3)
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | The aromatic hydrocarbon rubber filling oil company standard |
| The hydrogenation modifying process condition | ||||
| The hydrogen dividing potential drop, MPa | 9.0 | 11.0 | 13.0 | |
| Temperature of reaction, ℃ | 390 | 370 | 380 | |
| Volume space velocity, h -1 | 0.8 | 0.6 | 1.0 | |
| Hydrogen to oil volume ratio | 1000 | 1100 | 1200 | |
| Cut product property more than 360 ℃ | ||||
| Boiling range, ℃ | 362～520 | 363～521 | 364～523 | / |
| Density, 20 ℃, kg/m 3 | 1084.5 | 1082.8 | 1088.6 | ≮985.0 |
| Open flash point, ℃ | 233 | 231 | 235 | ≮220 |
| Pour point, ℃ | 19 | 18 | 20 | ≯25 |
| Viscosity, 100 ℃, mm 2/s | 23.04 | 22.86 | 23.25 | 20.0～26.0 |
| Refractive index, n D 20 | 1.5792 | 1.5768 | 1.5826 | 1.55～1.60 |
| Sulphur/nitrogen content, μ g/g | 368/826 | 352/786 | 375/844 | / |
| Aromaticity content, w% | 94.1 | 93.5 | 94.8 | ≮85.0 |
| Colloid and asphalt content, w% | 1.7 | 1.5 | 1.8 | / |
| Moisture, v% (v% represents percent by volume) | Do not have | Do not have | Do not have | ≯0.05 |
| Smell | Free from extraneous odour | Free from extraneous odour | Free from extraneous odour | / |
Claims (1)
1, a kind of production method of aromatic hydrocarbon rubber filling oil is characterized in that being made up of following steps:
A. coal tar fraction and hydrogen enter hydrogenator after mixing, with Mo-Ni-P catalyst for hydro-upgrading contact reacts, remove sulphur, nitrogen impurity and colloid, bituminous matter in the coal tar fraction, reaction conditions is: hydrogen dividing potential drop 8.0～14.0MPa, 370～390 ℃ of temperature of reaction, volume space velocity 0.6～1.0h
-1, hydrogen to oil volume ratio 1000～1200, reaction afterreaction product is derived hydrogenator;
Described Mo-Ni-P catalyst for hydro-upgrading, in oxide dry basis, MoO
3Account for 15～25w% of total catalyst weight, NiO accounts for 2～6w% of total catalyst weight, P
2O
5Account for 3～8w% of total catalyst weight, all the other are the amorphous silicic acid alumina supporter;
B. the reaction product that obtains of steps A enters gas delivery and stable system after heat exchange, cooling, isolate hydrogen, dry gas, hydrogen sulfide and ammonia and liquefied gas after, obtain product liquid;
C. the product liquid that step B is obtained carries out fractionation, cutting in separation column, obtains cut more than 360 ℃, and this cut is the aromatic hydrocarbon rubber filling oil product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510018058XA CN1331985C (en) | 2005-09-29 | 2005-09-29 | Method for producing aromatic hydrocarbon rubber filling oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510018058XA CN1331985C (en) | 2005-09-29 | 2005-09-29 | Method for producing aromatic hydrocarbon rubber filling oil |
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| Publication Number | Publication Date |
|---|---|
| CN1752182A true CN1752182A (en) | 2006-03-29 |
| CN1331985C CN1331985C (en) | 2007-08-15 |
Family
ID=36679188
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|---|---|---|---|
| CNB200510018058XA Expired - Fee Related CN1331985C (en) | 2005-09-29 | 2005-09-29 | Method for producing aromatic hydrocarbon rubber filling oil |
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| CN101386687B (en) * | 2008-10-24 | 2011-06-01 | 中国海洋石油总公司 | Aromatic rubber oil and producing method thereof |
| CN101386688B (en) * | 2008-10-24 | 2011-07-20 | 中国海洋石油总公司 | Aromatic rubber oil and producing method thereof |
| CN101250433B (en) * | 2008-03-28 | 2012-02-15 | 湖南长岭石化科技开发有限公司 | Coal tar hydrogenation technique |
| CN102453538A (en) * | 2010-10-14 | 2012-05-16 | 中国石油化工股份有限公司 | Production method of environmentally friendly tyre aromatic oil |
| CN102660325A (en) * | 2012-05-19 | 2012-09-12 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of environment-friendly rubber tire filling oil |
| CN102888243A (en) * | 2012-10-08 | 2013-01-23 | 陕西省能源化工研究院 | Coal tar tail oil fraction and application thereof |
| CN104203876A (en) * | 2012-04-10 | 2014-12-10 | 昭和电工株式会社 | Rubber compounding oil and method for manufacturing the same |
| CN104593065A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司 | Production method for environment-friendly rubber filling oil |
| CN104593066A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司 | Method for producing environment-friendly rubber filling oil from medium-low temperature coal tar |
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| CN1018662B (en) * | 1985-04-01 | 1992-10-14 | 西北给排水技术开发公司 | Improvement of water purification system |
| CN1022844C (en) * | 1989-09-11 | 1993-11-24 | 齐鲁石油化工公司研究院 | New technology for manufacturing high-value product by use of wax oil |
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| CN101386687B (en) * | 2008-10-24 | 2011-06-01 | 中国海洋石油总公司 | Aromatic rubber oil and producing method thereof |
| CN101386688B (en) * | 2008-10-24 | 2011-07-20 | 中国海洋石油总公司 | Aromatic rubber oil and producing method thereof |
| CN102453538A (en) * | 2010-10-14 | 2012-05-16 | 中国石油化工股份有限公司 | Production method of environmentally friendly tyre aromatic oil |
| CN102453538B (en) * | 2010-10-14 | 2014-08-20 | 中国石油化工股份有限公司 | Production method of environmentally friendly tyre aromatic oil |
| CN104203876A (en) * | 2012-04-10 | 2014-12-10 | 昭和电工株式会社 | Rubber compounding oil and method for manufacturing the same |
| CN102660325B (en) * | 2012-05-19 | 2014-04-23 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of environment-friendly rubber tire filling oil |
| CN102660325A (en) * | 2012-05-19 | 2012-09-12 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of environment-friendly rubber tire filling oil |
| CN102888243A (en) * | 2012-10-08 | 2013-01-23 | 陕西省能源化工研究院 | Coal tar tail oil fraction and application thereof |
| CN104593065A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司 | Production method for environment-friendly rubber filling oil |
| CN104593066A (en) * | 2013-11-04 | 2015-05-06 | 中国石油化工股份有限公司 | Method for producing environment-friendly rubber filling oil from medium-low temperature coal tar |
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| CN1331985C (en) | 2007-08-15 |
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Address after: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Patentee after: China Petrochemical Group Corp. Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group Patentee before: China Petrochemical Group Corp. |
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