CN201280527Y - Aromatic hydrocarbon production equipment - Google Patents
Aromatic hydrocarbon production equipment Download PDFInfo
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- CN201280527Y CN201280527Y CNU2008201727738U CN200820172773U CN201280527Y CN 201280527 Y CN201280527 Y CN 201280527Y CN U2008201727738 U CNU2008201727738 U CN U2008201727738U CN 200820172773 U CN200820172773 U CN 200820172773U CN 201280527 Y CN201280527 Y CN 201280527Y
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Abstract
The utility model belongs to the field of light hydrocarbon aromatization equipment, and particularly relates to an equipment system for producing aromatic hydrocarbon. The equipment system comprises a raw material preprocessor, a liquefied gas spherical tank and a C5 spherical tank, wherein, the liquefied gas spherical tank and the C5 spherical tank are connected with the raw material preprocessor. The equipment system is characterized in that both the liquefied gas spherical tank and the C5 spherical tank are connected with a feeding vaporizer; the feeding vaporizer is connected in series with a heating furnace, a fixed bed reactor and a gas-liquid separating tank in sequence; the gas phase outlet of the gas-liquid separating tank is connected with the inlet of an absorption tower; the liquid phase outlet of the gas-liquid separating tank is connected with the inlet of the desorption tower; both the liquid phase outlet of the absorption tower and the gas phase outlet of the desorption tower are connected with the inlet of the gas-liquid separating tank; and the desorption tower, a 5th carbon removal tower, a deheptanizer, a desilylation scrubber and an 8th carbon removal tower are connected in series and in sequence. The utility model has the advantages of simple operation, short maintenance period, good yield coefficient, high efficiency and easy popularization.
Description
Technical field
The utility model belongs to light-hydrocarbon aromatized apparatus field, is specifically related to a kind of device systems of producing aromatic hydrocarbons.
Background technology
At present, abroad some light-hydrocarbon aromatized technology have entered the industrial application stage.Domesticly also obtaining some progress aspect the light-hydrocarbon aromatized technical study, investigating the aromatization of propane on ZRP molecular sieve and silicon modification ZRP molecular sieve as petroleum science research institute (RIPP).On the ZRP molecular sieve, the xylene isomer in the product liquid is thermodynamic(al)equilibrium basically and distributes, and para-selectivity is poor; On silicon modification ZRP molecular sieve, with the increase of SiO2 content, the degree that the active centre of ZRP molecular sieve outer surface is capped increases, and the xylene isomer para-selectivity increases gradually in the product liquid, brings up to 13.3% from 4.1%.But do not find the report that full scale plant is built.
Qilu Petrochemical limited-liability company olefin plant is cooperated with Beijing petroleum science research institute, promptly began the feasibility of the aromizing of raffinating oil is studied from 1993, and carried out first industrial test in March, 1993, technical process carried out testing again after the suitable improvement in 1998.Raffinating oil is the aliphatic fraction of a kind of carbon five to carbon eight, test-results shows, raffinating oil as a kind of auxiliary material of producing aromatic hydrocarbons is feasible under certain condition, can not have side effects in the reaction process to isomerized main body reaction, it is opposite because the reaction of dehydrogenation aromatization has been offset isomerization reaction institute liberated heat for thermo-negative reaction, accelerated the carrying out of isomerization reaction to a certain extent, but catalyzer is the platiniferous noble metal catalyst, costs an arm and a leg.Not carrying out large-scale industrial production after the off-test, have certain problem on the technology, mainly is that yield is not high.
The Luoyang Petrochemical research institute that research is dropped into more energy has carried out more deep research to light-hydrocarbon aromatized technology, and developed relevant catalyzer, what its testing apparatus adopted is the catalyst fluidization bed technique of approximate catalytic reforming, but does not still have industrialized device to produce the report of high-purity petroleum purified petroleum benzin or toluene.
Dongming petrochemical industry adopts 50,000 tons of/year liquefied petroleum gas (LPG) of Luoyang Petrochemical research institute technology building one cover to produce the device of aromatic hydrocarbons, reactor adopts the fluidisation regeneration techniques, liquid yield has only about 45%, effect is general, simultaneously owing to there are not the later separation means, and oil purified petroleum benzin, toluene that can't the output GB, adding dry gas can't make full use of, liquid phase can only be used for mixing gasoline, and economic benefit is not high, is in end-of-life stage.
Danyang petrochemical industry aromatization process for splitting SC-cut applicable raw materials scope relative narrower is used the expensive catalyzer that contains gallium, and the one way reaction times is short, and three benzaldehyde products can't be realized high purity.
Lower carbon number hydrocarbons (the C of Fusun PetroleumCollege's research
2-C
5) the catalyzer cost that uses of technology of aromatization is low, but its same fixed bed reaction system that adopts with Danyang petrochemical iy produced technology, catalyzed reaction and catalyst regeneration hocket, and need switching time, have weakened production efficiency.Can not the high-purity GB petroleum benzene of output, toluene.
The aromizing research that with methane is raw material also is in the laboratory study stage at present.
The utility model content
Cheap C such as the purpose of this utility model provides and a kind ofly make use of liquefied petroleum gas, pyrolysis gasoline, oil natural gas, associated gas and refinery gas
3～C
8The light hydrocarbon resource prepares the device systems of the production aromatic hydrocarbons of high-purity GB petroleum benzene, toluene and the dimethylbenzene of high value and dry gas byproduct.
The utility model is achieved through the following technical solutions:
It is a kind of device systems of producing aromatic hydrocarbons, comprise the raw materials pretreatment device, lpg spherical tank that is connected with the raw materials pretreatment device and carbon five spherical tanks, it is characterized in that lpg spherical tank all is connected with the charging vaporizer with carbon five spherical tanks, charging vaporizer and process furnace, fixed-bed reactor, knockout drum is connected in series successively, the gaseous phase outlet of knockout drum is connected with the import on absorption tower, the liquid phase outlet of knockout drum is connected with the import of desorption tower, the liquid phase outlet on absorption tower, the gaseous phase outlet of desorption tower all is connected with the import of knockout drum, desorption tower, decarburization five towers, deheptanizer, take off toluene tower, decarburization eight towers are connected in series successively.
The branch of the gaseous phase outlet of knockout drum finally is connected with the process furnace import.
The branch of the outlet of deheptanizer is connected with the liquid phase import on absorption tower.
Principle of work of the present utility model is as follows:
After the gasification of charging vaporizer, enter process furnace through the light hydrocarbon feedstocks of impurity pretreatment and be warming up to 450-570 ℃, enter fixed-bed reactor then from top to bottom, under the effect of extraordinary DLP-1 type catalyzer, carry out aromatization, 450 ℃-600 ℃ of temperature of reaction, pressure 0-0.4MPa, air speed 0.4-0.8h
-1Wherein most of feedstock conversion is aromatic components such as benzene,toluene,xylene, generates rich olefins dry gas such as hydrogen, methane, ethene, propane, propylene simultaneously.The reaction after product is delivered to knockout drum and is carried out gas-liquid separation after a series of heat exchange and cooling, and gas phase after the separation and liquid phase enter the desorb that absorption tower and desorption tower carry out light constituent in the recovery of heavy constituent in the gas phase and the heavy constituent respectively.Liquid phase aromatic hydrocarbons mixture after the desorb enters and can obtain the needed benzene mixed product of aromatic extraction unit after depentanizer further removes wherein carbon five lighting ends, and benzene mixed promptly obtains oil purified petroleum benzin, toluene and the dimethylbenzene product of GB after the tetramethylene sulfone extracting.Rich olefins dry gas feeder gas holder after absorption agent absorbs stores, and is sent to ethylene unit user outside the battery limit (BL) behind the compressed machine pressure-raising.
The utlity model has following advantage:
1) connection of knockout drum, absorption tower, desorption tower has realized a kind of new dry gas separation method, dry gas yield height.
2) utilize the circulation dry gas to do carrier gas, prolong reaction time and catalyst life.
3) raw material of Shi Yonging extensively, be easy to promote.Comprised from carbon three to carbon all hydrocarbon components of eight, and conventional aromatization generally can only be handled carbon four, C5 fraction.
4) simple to operate, maintenance intervals weak point.Reactor adopts fixed-bed reactor, and simple than fluidized bed process, catalyst abrasion is little, and the recovery time is short.
5) the product separation kind is many, purity is high.The utility model can the highly purified GB petroleum benzene of disposable output (99.99%), toluene (99.90%), enterprise's mark dimethylbenzene and raffinate oil, and traditional technology can only be produced aromatic hydrocarbons mixture or add gasoline, benzene, the toluene purity of producing are low, reach the GB difficulty.
Through experiment, liquid yield reaches more than 55% behind use the utility model, and the dry gas yield is 45%.The weight space velocity of reaction reaches more than 0.4, and lighter hydrocarbons (liquefied petroleum gas (LPG) etc.) transformation efficiency reaches more than 90%, is much better than traditional technology.
Description of drawings
Accompanying drawing is a structural representation of the present utility model.
As shown in FIG.: 1 raw materials pretreatment device; 2 lpg spherical tanks; 3 carbon, five spherical tanks; 4 charging vaporizers; 5 process furnace; 6 fixed-bed reactor; 7 knockout drums; 8 decarburizations, eight towers; 9 take off toluene tower; 10 deheptanizers; 11 decarburizations, five towers; 12 desorption towers; 13 absorption towers.
Embodiment
Is that example elaborates the utility model below in conjunction with accompanying drawing with liquefied petroleum gas (LPG), cracking c_5.
As shown in drawings, raw materials pretreatment device 1 is connected with carbon five spherical tanks 4 with lpg spherical tank 2 respectively, lpg spherical tank 2 all is connected with charging vaporizer 4 with carbon five spherical tanks 3, charging vaporizer 4 and process furnace 5, fixed-bed reactor 6, knockout drum 7 is connected in series successively, the gaseous phase outlet of knockout drum 7 is connected with the import on absorption tower 13, the branch of the gaseous phase outlet of knockout drum 7 is connected with process furnace 5 imports, the liquid phase outlet of knockout drum 7 is connected with the import of desorption tower 12, the liquid phase outlet on absorption tower 13, the gaseous phase outlet of desorption tower 12 all is connected with the import of knockout drum 7, desorption tower 12, decarburization five towers 11, deheptanizer 10, take off toluene tower 9, decarburization eight towers 8 are connected in series successively, and the branch of the outlet of deheptanizer 10 is connected with the liquid phase import on absorption tower 13.
When the utility model uses, through raw materials pretreatment device 1 pretreated C4/C5 raw material, single or be mixed into charging vaporizer 4 after enter fixed-bed reactor 6 from top to bottom after process furnace 5 heating, reaction oil gas hot water in waste heat boiler carries out heat exchange and produces middle pressure steam, after further heat exchange, cooling, enter knockout drum 7 and carry out gas-oil separation, isolated reaction gas enters the further absorption extraction in 13 bottoms, the absorption tower C that coagulates wherein by gaseous phase outlet
5Above hydro carbons, absorption agent are the C from deheptanizer 10
8-C
10Cut and from a part of C of extracting Cutting Tap
8-C
10Cut.Enter knockout drum 7 after the cooling of absorption tower 13 bottoms, the dry gas of cat head enters gas holder, after the lime set jar before and after the gas holder reclaims wherein possible lime set as the byproduct carrying device.Knockout drum 7 isolated reaction solutions enter desorption tower 12, enter knockout drum 7 after the cooling of desorption tower 12 top gas, desorption tower 12 bottoms enter depentanizer and remove pentane cut and recovery from the top, bottoms is removed deheptanizer 10 and to be mixed aromatic hydrocarbons from cat head and be sent to and mix the refining pure benzene,toluene,xylene of GB of benzene solvent tripping device, tower bottom distillate and a part of C from the crude benzol solvent separation unit
8C
10Cut mixes, and a part enters 13 tops, absorption tower as absorbing stripping liquid, and most of entering as the charging of taking off toluene tower taken off toluene tower 9, and the cat head toluene component is sent into extraction plant, and tower base stream is sent to decarburization eight towers 8 and obtained smart dimethylbenzene and heavy aromatics product.
The technical performance contrast of the utility model and same device is as follows:
(1) reaction effect
| Performance indications | Design load | Actual value | The technical performance that reaches | Remarks |
| The liquid phases of reactants yield, % | 55 | 58.5 | Reach | Weight ratio |
| Reactant gas phase yield, % | 45 | 41.5 | Reach | Weight ratio |
| Reaction conversion ratio, % | 90 | 95 | Arrive | Weight ratio |
| Air speed | 0.4-0.8 | 0.4 | Reach | No high-speed test |
| Reaction temperature, ℃ | 450-600 | 520 | Reach | Mean value |
| Reaction pressure, MPa | 0-0.4 | 0.169 | Reach | Gauge pressure |
| Regeneration period, hour | 168 | 400 | Arrive | The raw material difference |
| Catalyst life | 1 year | — | — | Not yet due |
(2) product quality indicator
| Name of product | Purity, % | The GB requirement | Comparing result | Other index situation |
| Purified petroleum benzin | 99.99 | (99.30 top grade) | Be higher than GB | Reach GB |
| Toluene | 99.9 | (99.7 top grade) | Be higher than GB | Reach GB |
(3) with domestic same device contrast
| Performance indications | Design load | Actual value | Domestic same device | Remarks |
| The liquid phases of reactants yield, % | 55 | 58.5 | 47.5 | |
| Reactant gas phase yield, % | 45 | 41.5 | 52.5 | |
| Reaction conversion ratio, % | 90 | 95 | 85 | |
| Air speed | 0.4-0.8 | 0.4 | 0.4 | |
| Reaction temperature, ℃ | 450-600 | 520 | 510 | |
| Reaction pressure, MPa | 0-0.4 | 0.169 | 0.2 | |
| Regeneration period, hour | 168 | 400 | Cyclic regeneration | Fluid bed |
| Catalyst life | 1 year | — | — | |
| The liquid-phase product bromine index | 1000 | 500-650 | 650 | mg/100gBr |
| Benzaldehyde product purity, % | 99.96 | 99.96-99.99 | 99.0 | |
| The toluene product purity, % | 99.7 | 99.8-99.99 | 95 | |
| Sulfur content, ppm | 1 | 1 | 1 |
As can be seen from the above table: no matter from reaction effect or product quality, the utility model surpasses domestic same device comprehensively, Wherein liquid yield and product quality are particularly evident.
Claims (3)
1, a kind of device systems of producing aromatic hydrocarbons, comprise the raw materials pretreatment device, lpg spherical tank that is connected with the raw materials pretreatment device and carbon five spherical tanks, it is characterized in that lpg spherical tank all is connected with the charging vaporizer with carbon five spherical tanks, charging vaporizer and process furnace, fixed-bed reactor, knockout drum is connected in series successively, the gaseous phase outlet of knockout drum is connected with the import on absorption tower, the liquid phase outlet of knockout drum is connected with the import of desorption tower, the liquid phase outlet on absorption tower, the gaseous phase outlet of desorption tower all is connected with the import of knockout drum, desorption tower, decarburization five towers, deheptanizer, take off toluene tower, decarburization eight towers are connected in series successively.
2, the device systems of production aromatic hydrocarbons according to claim 1 is characterized in that the branch of the gaseous phase outlet of knockout drum is connected with the process furnace import.
3, the device systems of production aromatic hydrocarbons according to claim 1 is characterized in that the branch of the outlet of deheptanizer is connected with absorption tower liquid phase import.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201727738U CN201280527Y (en) | 2008-10-09 | 2008-10-09 | Aromatic hydrocarbon production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201727738U CN201280527Y (en) | 2008-10-09 | 2008-10-09 | Aromatic hydrocarbon production equipment |
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| Publication Number | Publication Date |
|---|---|
| CN201280527Y true CN201280527Y (en) | 2009-07-29 |
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| CNU2008201727738U Expired - Fee Related CN201280527Y (en) | 2008-10-09 | 2008-10-09 | Aromatic hydrocarbon production equipment |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101857808A (en) * | 2010-06-17 | 2010-10-13 | 宁夏宝塔石化集团有限公司 | Method for preparing gasoline from liquefied gas through aromatization and fixed bed reactor |
| CN101880546A (en) * | 2010-06-25 | 2010-11-10 | 山东齐旺达集团海仲化工科技有限公司 | Method for improving quality and reaction period in production of gasoline by using low-carbon hydrocarbons |
| CN102399578A (en) * | 2010-09-08 | 2012-04-04 | 宁夏宝塔石化集团有限公司 | Preposed condensation separation method and device for preparing gasoline by aromatization of liquefied gas |
| CN108017492A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | The method of mixed light-hydrocarbon aromatization aromatic hydrocarbons |
| CN108144318A (en) * | 2018-02-01 | 2018-06-12 | 南京英斯派工程技术有限公司 | A kind of associated gas desulphurization system |
-
2008
- 2008-10-09 CN CNU2008201727738U patent/CN201280527Y/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101857808A (en) * | 2010-06-17 | 2010-10-13 | 宁夏宝塔石化集团有限公司 | Method for preparing gasoline from liquefied gas through aromatization and fixed bed reactor |
| CN101857808B (en) * | 2010-06-17 | 2014-02-26 | 宁夏宝塔石化集团有限公司 | Method for preparing gasoline from liquefied gas through aromatization and fixed bed reactor |
| CN101880546A (en) * | 2010-06-25 | 2010-11-10 | 山东齐旺达集团海仲化工科技有限公司 | Method for improving quality and reaction period in production of gasoline by using low-carbon hydrocarbons |
| CN102399578A (en) * | 2010-09-08 | 2012-04-04 | 宁夏宝塔石化集团有限公司 | Preposed condensation separation method and device for preparing gasoline by aromatization of liquefied gas |
| CN102399578B (en) * | 2010-09-08 | 2014-02-26 | 宁夏宝塔石化集团有限公司 | Pre-condensation-separation method in preparing gasoline through aromatization of liquefied gas and device thereof |
| CN108017492A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | The method of mixed light-hydrocarbon aromatization aromatic hydrocarbons |
| CN108144318A (en) * | 2018-02-01 | 2018-06-12 | 南京英斯派工程技术有限公司 | A kind of associated gas desulphurization system |
| CN108144318B (en) * | 2018-02-01 | 2023-12-19 | 南京佳华科技股份有限公司 | Associated gas desulfurization system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SHANDONG DAQI CHEMICAL TECHNOLOGY CO., LTD. Free format text: FORMER NAME: SHANDONG QIWANGDA GROUP HAIZHONG CHEMICAL INDUSTRY TECHNOLOGY CO., LTD. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: Jinling town Linzi District South Road East 255410 ene in Shandong province Zibo City Patentee after: Shandong Daqi Chemical Technology Co., Ltd. Address before: Jinling town Linzi District South Road East 255410 ene in Shandong province Zibo City Patentee before: Shandong Qiwangda Group Haizhong Chemical Industry Technology Co., Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090729 Termination date: 20161009 |