CN1478862A - Method of removing organic silicon compound from distillate oil - Google Patents
Method of removing organic silicon compound from distillate oil Download PDFInfo
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- CN1478862A CN1478862A CNA021290431A CN02129043A CN1478862A CN 1478862 A CN1478862 A CN 1478862A CN A021290431 A CNA021290431 A CN A021290431A CN 02129043 A CN02129043 A CN 02129043A CN 1478862 A CN1478862 A CN 1478862A
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Abstract
A process for removing organic silicon compound from fractional oil features that the fractional oil passes through the adsorbent bed at 90-200 deg.C under 0.2-0.6 MPa to remove said organic silicon compound. Said adsorbent is composed of alumina and silicon oxide, and can be regenerated by alcohol contained alkali solution for continuous operation.
Description
Technical field
The present invention is a kind of method that efficiently removes silicon-containing compound from distillate.Specifically, be a kind of method that adopts adsorption method of separation to remove the silicoorganic compound in the distillate.
Background technology
Outstanding day by day along with problem of environmental pollution, more strict environmental protection policy has been launched respectively in countries in the world.Therefore, require the refinery to produce the clean fuel of sulphur, " environmental friendliness " that nitrogen compound content is lower.The main method that reduces sulphur, amount of nitrides is hydrofining; And catalytic reforming is to improve the important means of quality of gasoline.Along with the poor qualityization of crude oil, a large amount of hydrogenation, reforming raw oil have generally used siliceous froth suppressor from delay coking process in this technology, cause low-molecular-weight silicoorganic compound mainly to be distributed in gasoline, the diesel oil distillate scope.The hydrogenation, reforming catalyst that with the aluminum oxide are carrier are when handling this type of distillate, usually because of having adsorbed the permanent poisoning and deactivation of a large amount of silicon-containing compounds.So the silicon-containing compound in effective elimination hydrogenation or the reformer feed is the effective ways that guarantee hydrogenation, reformer safe handling.
USP4,176,047 disclose and have a kind ofly removed the method for silicoorganic compound by absorption from coker gasoline, and described sorbent material is selected from aluminum oxide, activated alumina or useless desulfurization catalyst.The adsorption operations temperature is at least 90 ℃, preferred 120～150 ℃.When service temperature is 93 ℃, use depleted with the cobalt-molybdenum desulfurization catalyst of aluminum oxide as carrier, the silicone content of coker gasoline can be reduced to 2ppm from 5ppm.
USP4,343,693 disclose a kind of cubic meter of stone method that removes impurity such as sulfonate, silicone oil from feed stream.Described feed stream is to comprise C
5～C
10The oil fuel of hydro carbons.This patent use cheap and effectively silicon oxide (Davision59) and bauxitic clay be sorbent material, compare with expensive silica gel, can reduce running cost.
US6,248,230B1 discloses a kind of method for preparing clean fuel.This method with boiling range be 110～560 ℃ hydrocarbon feed before hydrogenation, remove natural polar compound wherein earlier.Described natural polar compound (NPC) refers to naturally occurring material in the petroleum fractions and the additive or the pharmaceutical chemicals of non-artificial interpolation, mainly refer to have the oxygenatedchemicals of polar group, as phenol, naphthenic acid, heterocyclic nitrogen compounds, as carbazole, draw diindyl, pyrimidine, quinoline etc., and aromatic hydroxy compound.The content of above-mentioned natural polar compound in petroleum fractions is 0.1～5.0 heavy %, and comprising the oxygenatedchemicals of 5.0～50 heavy % and the nitrogenous heterogeneous ring compound of 5.0～50 heavy %, its sulphur content is in the scope of 0.1～5.0 heavy %.This method uses absorption or method of extraction to remove NPC, its sorbent material of selecting for use comprises silica gel (silica gel), acidic white earth, Fuller's earth, gac, molecular sieve, aluminium hydroxide, ion exchange resin, activated alumina, and preferred aperture is that 40～200 , pore volume are the silica gel of 0.5～1.5cc/g.The strippant that this method is used is selected from the following ketone of alcohol, ether or six carbon, as methyl alcohol, methyl tertiary butyl ether and acetone.
Summary of the invention
The purpose of this invention is to provide a kind of method of utilizing the silicoorganic compound in the adsorption separating method effective elimination distillate.
The sorbent material that the present invention makes aluminum oxide and silicon oxide after composite by a certain percentage, the silicoorganic compound in can the active adsorption distillate, thus remove such impurity in the distillate.This sorbent material can use repeatedly with the regeneration of alkali lye wash-out, and is easy and simple to handle, is easy to realize continuous and stable production.
Description of drawings
Fig. 1 is the schematic flow sheet of the inventive method.
Embodiment
The method that from distillate, removes silicoorganic compound of the present invention, comprise with described distillate under 90～200 ℃, 0.2～0.6MPa by adsorbent bed, adsorbing and removing silicoorganic compound wherein, described sorbent material is made up of the aluminum oxide of 70～90 heavy % and the silicon oxide of 10～30 heavy %.
Sorbent material described in the aforesaid method is by aluminum oxide and silicon oxide is composite forms, and its compound method is by described mixed, then 150～250 ℃ of dryings with both.Be 1～6 hour suitable time of drying.The preferred gama-alumina of described aluminum oxide, preferred gama-alumina specific surface is 130～310 meters
2/ gram, pore volume are 0.2～0.7 milliliter/gram, and mean pore size is 40～115 .Preferred silicon oxide mean pore size is 30～50 , and specific surface is 300～500 meters
2/ gram, pore volume are 0.4～0.5 milliliter/gram.The pore volume of described two kinds of oxide compounds all is difficult for excessive, otherwise exists too much aperture will be unfavorable for the absorption of silicoorganic compound in the sorbent material.
Described distillate is the coking distillate of 80～400 ℃ of boiling ranges or the mixture of coking distillate and catalytic cracking distillate or virgin oil, and its silicone content is 20～800 mcg/ml.Described coking distillate comprises that coker gasoline, coker gas oil and boiling range are 330～400 ℃ coking distillate, and catalytic cracking distillate and virgin oil comprise the distillate of gasoline fraction, diesel oil distillate and 330～400 ℃.
The silicoorganic compound that contain in the coking distillate are in the delayed coking process, for avoiding the main component of the defoamer that coking material foaming introduces, are mainly the silicoorganic compound of polysiloxane fracture generation.This material can make follow-up hydrogenation catalyst or reforming catalyst poison and inactivation, so should limit its content.Silicone content should be less than 1 mcg/ml in the general requirement hydrogenation or the stock oil that uses of reforming.
Described absorption desiliconization temperature should be decided according to the boiling range of distillate, for the preferred adsorption temp of gasoline fraction is 90～105 ℃, and to the petrol and diesel oil mixed fraction, preferred adsorption temp is 150～170 ℃, to diesel oil distillate, preferred adsorption temp is 150～180 ℃.Distillate is 0.1～8.0 o'clock by adsorbent bed volume space velocity during adsorption operations
-1, preferred 0.5～2.0 o'clock
-1
After described adsorbents adsorb is saturated, adopting the alkali lye flushing to make adsorbent reactivation, is that desorbing agent makes silicon compound desorption from sorbent material by flushing with alkali lye promptly.Described alkali lye is the KOH or the NaOH aqueous solution that contain 5～15 heavy % ethanol and 15～25 heavy % trimethyl carbinols of pH value 8～10.
Above-mentioned desorption temperature is 80～100 ℃, and pressure is 0.2～0.8MPa, and using the volume space velocity of alkali lye flushing is 2.0～10.0 o'clock
-1, preferred 2.0～5.0 o'clock
-1Sorbent material behind the desorption purges down to doing and can reuse at 140～160 ℃ with nitrogen, and suitable purge time is 1～3 hour, and nitrogen pressure is 0.6～0.9MPa.
The inventive method is applicable to the silicoorganic compound that remove in the distillate, distillate after the desiliconization is carried out hydrotreatment, can prolong the work-ing life of hydrogenation catalyst, wherein the gasoline fraction after the desiliconization also can prolong the work-ing life of reforming catalyst as catalytic reforming raw material.
Use method provided by the invention, can effectively remove the silicoorganic compound in the distillate, and be easy to realize the continuous desiliconizing operation.As shown in Figure 1, the distillate that is stored in the distillate storage tank 11 enters first adsorption tower 12 through pipeline 10 from the top, silicoorganic compound in the distillate are being adsorbed when adsorbent bed, and the distillate after the desiliconization is discharged after pipeline 17 enters refining distillate storage tank 16 at the bottom of by adsorption tower.When treating that effluent in this adsorption tower reaches certain silicone content, represent its state that reached capacity, cut second adsorption tower 13 with distillate and proceed the desiliconization processing this moment, simultaneously the fresh alkali lye in the alkali lye storage tank 14 is entered the first sorbent material top of tower from pipeline 19, make the sorbent material desorption with the alkali lye flushing.The waste lye of discharging at the bottom of the adsorption tower enters the waste tank 15 through pipeline 18, discharges after environmental protection treatment.After alkali lye flushing finishes, adsorbent bed with nitrogen purging to dry, when the sorbent material for the treatment of second adsorption tower reaches capacity, again with the distillate incision to first adsorption tower, with alkali lye the sorbent material in second adsorption tower 13 after saturated is regenerated simultaneously.So circulation is adsorbed and the regenerated operation, can continous-stable remove silicoorganic compound in the distillate.
Sorbent material in the described adsorption tower can be distributed into 1～4 bed.When load in the contactor adsorbent bed be two when above, the sectional filling, promptly adjacent two beds have certain space.
Below by example in detail the present invention, but the present invention is not limited to this.
Example 1
(1) preparation sorbent material
γ-Al with 90 heavy %
2O
3The silicon oxide (Haiyang Chemical Plant, Qingdao) of (Shanghai the May 4th chemical reagent factory) and 10 heavy % mixes the back and made sorbent material I in 3 hours in 200 ℃ of dryings, and raw materials used rerum natura sees Table 1.
(2) absorption desiliconization
In first adsorption tower 12 and second adsorption tower 13, load the sorbent material I of 100ml (94.5 gram) respectively, be preheated to 98 ℃.It is standby that the pH value that will contain 10% ethanol and 20% trimethyl carbinol is that 9 NaOH solution injects alkali lye storage tank 14.
30% coker gasoline and 70% straight-run spirit mixture are put into distillate storage tank 11, its boiling range is 80～205 ℃, silicone content is 500 mcg/ml, and silicon compound wherein is the small molecules silicoorganic compound that coking defoamer CDF-10A (the emerging general fine chemical technology in Beijing development company produces) obtains 500 ℃ of cracking.Distillate storage tank 11 is preheated to 98 ℃, pressure is adjusted into 0.2MPa, feed volume air speed by 0.8 is injected first adsorption tower 12 with above-mentioned siliceous gasoline, make it to have an effect with sorbent material I, when the silicone content of effluent surpasses 20 mcg/ml, think that promptly the sorbent material in the adsorption tower is saturated, stop the absorption desiliconization of this tower this moment, simultaneously the fresh alkali lye for preparing in the alkali lye storage tank 14 is injected first adsorption tower 12 and carry out the organosilicon desorption manipulation, desorption temperature is 85 ℃, alkali lye volume space velocity 3.0, pressure 0.3MPa when the silicone content of effluent is lower than 10 mcg/ml after 8 hours, stops to inject alkali lye, adsorption tower 12 is warming up to 150 ℃, and feeding pressure is that the nitrogen of 0.7MPa blows 2 hours to dry.And then organosilicon gasoline solution switched to first adsorption tower 12 that finishes of regeneration, it is saturated once more to sorbent material to continue to adsorb desiliconization by aforementioned condition.Silicon loading capacity before and after the adsorbent reactivation sees Table 2, and wherein adsorption time is the time that sorbent material reaches capacity.
Example 2
Method by example 1 prepares sorbent material II, and that different is γ-Al in the sorbent material
2O
3Content be 80 heavy %, the content of silicon oxide is 20 heavy %.
With sorbent material II pack into first adsorption tower 12 and second adsorption tower 13, adsorb the desiliconization operation by the method for example 1, the results are shown in Table 2.
Example 3
Method by example 1 prepares sorbent material III, and that different is γ-Al in the sorbent material
2O
3Content be 70 heavy %, the content of silicon oxide is 30 heavy %.
With sorbent material III pack into first adsorption tower 12 and second adsorption tower 13, adsorb the desiliconization operation by the method for example 1, the results are shown in Table 2.
Example 4
Use sorbent material I to adsorb desiliconization by the method for example 1, the different raw materials that is to use is the mixture of 30% coker gas oil and 70% straight-run diesel oil, and boiling range is 192～400 ℃, and silicone content is 500 mcg/ml, and silicon compound is originated with example 1.During adsorption operations two adsorption towers and distillate storage tank 11 all are preheated to 180 ℃, during desorption manipulation temperature are transferred to 90 ℃, the results are shown in Table 2.
Example 5
Adsorb the desiliconization operation by the method for example 4, that different is the sorbent material II that packs in adsorption tower, the results are shown in Table 2.
Example 6
Adsorb the desiliconization operation by the method for example 4, that different is the sorbent material III that packs in adsorption tower, the results are shown in Table 2.
Example 7
Use sorbent material I to adsorb desiliconization by the method for example 1, the different raw materials that is to use is the mixture of 30% coking distillate and 70% straight-run diesel oil, and boiling range is 76～400 ℃, and silicone content is 500 mcg/ml, and silicon compound is originated with example 1.During adsorption operations two adsorption towers and distillate storage tank 11 all are preheated to 170 ℃, during desorption manipulation temperature are transferred to 90 ℃.The results are shown in Table 2.
Example 8
Adsorb the desiliconization operation by the method for example 7, that different is the sorbent material II that packs in adsorption tower, the results are shown in Table 2.
Example 9
Adsorb the desiliconization operation by the method for example 7, that different is the sorbent material III that packs in adsorption tower, the results are shown in Table 2.
Comparative Examples 1
Pressing the method for example 1, is that sorbent material adsorbs the desiliconization operation with silicon oxide, the results are shown in Table 2.
Comparative Examples 2
Pressing the method for example 4, is that sorbent material adsorbs the desiliconization operation with the gama-alumina described in the example 1 respectively, the results are shown in Table 2.
By table 2 data as can be known, use simple silicon oxide to be sorbent material, the adsorption time of fresh dose and regenerator is all shorter, illustrates that its absorption property compares all relatively poor with regenerability with sorbent material of the present invention.And be sorbent material with simple aluminum oxide, though fresh dose absorption property is suitable with sorbent material of the present invention, the regenerator poor-performing.Table 2 data illustrate that also the loading capacity of sorbent material of the present invention improves with the raising of adsorption temp, that is to say, sorbent material of the present invention is more suitable for using under higher temperature, and alumina content wherein should not be low excessively.
Table 1
Table 2
| Project | Specific surface, rice 2/ gram | Pore volume, milliliter/gram | Mean pore size, |
| Silicon oxide | ????476 | ????0.45 | ???????40 |
| ?γ-Al 2O 3 | ????260 | ????0.61 | ???????75 |
| Instance number | Raw material | The sorbent material numbering | Loading capacity, gram silicon/kilogram sorbent material | Adsorption time, hour | ||
| Fresh dose | Regenerator | Fresh dose | Regenerator | |||
| ??1 | Gasoline fraction | ?I | ???7.31 | ????6.50 | ????18 | ????16 |
| ??2 | Gasoline fraction | ?II | ???9.31 | ????8.46 | ????22 | ????20 |
| ??3 | Gasoline fraction | ?III | ???7.20 | ????6.30 | ????16 | ????14 |
| ??4 | Diesel oil distillate | ?I | ???11.38 | ????10.57 | ????28 | ????26 |
| ??5 | Diesel oil distillate | ?II | ???16.93 | ????15.24 | ????40 | ????36 |
| ??6 | Diesel oil distillate | ?III | ???15.30 | ????13.50 | ????34 | ????30 |
| ??7 | The petrol and diesel oil mixture | ?I | ???11.38 | ????10.57 | ????32 | ????30 |
| ??8 | The petrol and diesel oil mixture | ?II | ???14.39 | ????12.70 | ????34 | ????30 |
| ??9 | The petrol and diesel oil mixture | ?III | ???13.51 | ????11.70 | ????30 | ????26 |
| Comparative Examples 1 | Gasoline fraction | Silicon oxide | ???4.11 | ????1.03 | ????8 | ????2 |
| Comparative Examples 2 | Diesel oil distillate | Gama-alumina | ???11.50 | ????5.75 | ????32 | ????16 |
Claims (7)
1, a kind of method that from distillate, removes silicoorganic compound, comprise with described distillate under 90～200 ℃, 0.2～0.6MPa by adsorbent bed, adsorbing and removing silicoorganic compound wherein, described sorbent material is made up of the aluminum oxide of 70～90 heavy % and the silicon oxide of 10～30 heavy %.
2, in accordance with the method for claim 1, it is characterized in that described aluminum oxide is a gama-alumina, its specific surface is 130～3 10 meters
2/ gram, pore volume are 0.2～0.7 milliliter/gram, and mean pore size is 40～115 , and the mean pore size of silicon oxide is 30～50 , and specific surface is 300～500 meters
2/ gram, pore volume are 0.4～0.5 milliliter/gram.
3, in accordance with the method for claim 1, it is characterized in that described adsorption temp is 150～180 ℃, distillate is 0.1～8.0 o'clock by adsorbent bed volume space velocity
-1
4, in accordance with the method for claim 1, it is characterized in that described distillate is the coking distillate of 80～400 ℃ of boiling ranges or the mixture of coking distillate and catalytic cracking distillate or virgin oil, its silicone content is 1～800 mcg/ml.
5, in accordance with the method for claim 1, it is characterized in that described silicoorganic compound are the silicoorganic compound that the polysiloxane fracture produces.
6, in accordance with the method for claim 1, after it is characterized in that described adsorbents adsorb is saturated, adopting the alkali lye flushing to make sorbent material desorption and regeneration, described alkali lye is the KOH or the NaOH aqueous solution that contain 5～15 heavy % ethanol and 15～25 heavy % trimethyl carbinols of pH value 8～10.
7, in accordance with the method for claim 6, it is characterized in that described desorption temperature is 80～100 ℃, pressure is 0.2～0.8MPa, and the volume space velocity of used flushing alkali lye is 2.0～10.0 o'clock
-1
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|---|---|---|---|
| CNB021290431A CN1191328C (en) | 2002-08-29 | 2002-08-29 | Method of removing organic silicon compound from distillate oil |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101343566B (en) * | 2007-07-09 | 2012-08-29 | 中国石油化工股份有限公司 | Method for improving running period of hydrogenation plant for poor petroleum naphtha |
| CN101869830B (en) * | 2009-04-22 | 2013-01-30 | 北京三聚环保新材料股份有限公司 | Method for preparing silicon-aluminium denitrfying agent |
| CN101186839B (en) * | 2006-10-18 | 2013-03-27 | Ifp公司 | Use of alumina as adsorption agent for removing organometallic silicon complexes |
| CN101555417B (en) * | 2008-09-04 | 2013-09-04 | 北京三聚环保新材料股份有限公司 | Denitrifier and preparation method thereof |
| CN104492450A (en) * | 2014-12-24 | 2015-04-08 | 武汉科林精细化工有限公司 | Coked gasoline desilication catalyst and preparation method thereof |
| CN105085757A (en) * | 2014-04-22 | 2015-11-25 | 中国石油化工股份有限公司 | Ethylene-alpha olefin-non-conjugated dialkene copolymer and preparation method thereof |
| CN105617993A (en) * | 2015-12-10 | 2016-06-01 | 湖南科技大学 | Regeneration method of spent lubrication oil adsorbent |
| CN109152978A (en) * | 2016-05-31 | 2019-01-04 | 美国陶氏有机硅公司 | Use the method and apparatus for carrying out this method of volatile component in the elastomer adsorbent depletion mixture of crosslinking |
| CN110382083A (en) * | 2017-03-14 | 2019-10-25 | 美国陶氏有机硅公司 | Use the method and apparatus for carrying out this method of the organosilicon composition in adsorbent copolymer depletion mixture |
| WO2022135944A3 (en) * | 2020-12-21 | 2022-08-18 | IFP Energies Nouvelles | Method for capturing silicon at low hourly space velocity |
-
2002
- 2002-08-29 CN CNB021290431A patent/CN1191328C/en not_active Expired - Lifetime
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101186839B (en) * | 2006-10-18 | 2013-03-27 | Ifp公司 | Use of alumina as adsorption agent for removing organometallic silicon complexes |
| CN101343566B (en) * | 2007-07-09 | 2012-08-29 | 中国石油化工股份有限公司 | Method for improving running period of hydrogenation plant for poor petroleum naphtha |
| CN101555417B (en) * | 2008-09-04 | 2013-09-04 | 北京三聚环保新材料股份有限公司 | Denitrifier and preparation method thereof |
| CN101869830B (en) * | 2009-04-22 | 2013-01-30 | 北京三聚环保新材料股份有限公司 | Method for preparing silicon-aluminium denitrfying agent |
| CN105085757B (en) * | 2014-04-22 | 2017-12-19 | 中国石油化工股份有限公司 | A kind of ethylene-alpha-olefin non-conjugated diene hydrocarbon copolymer and preparation method thereof |
| CN105085757A (en) * | 2014-04-22 | 2015-11-25 | 中国石油化工股份有限公司 | Ethylene-alpha olefin-non-conjugated dialkene copolymer and preparation method thereof |
| CN104492450A (en) * | 2014-12-24 | 2015-04-08 | 武汉科林精细化工有限公司 | Coked gasoline desilication catalyst and preparation method thereof |
| CN104492450B (en) * | 2014-12-24 | 2016-09-21 | 武汉科林精细化工有限公司 | A kind of coker gasoline desilicification catalyst and preparation method thereof |
| CN105617993A (en) * | 2015-12-10 | 2016-06-01 | 湖南科技大学 | Regeneration method of spent lubrication oil adsorbent |
| CN105617993B (en) * | 2015-12-10 | 2018-08-10 | 湖南科技大学 | A kind of regeneration method of waste lubricating oil adsorbent |
| CN109152978A (en) * | 2016-05-31 | 2019-01-04 | 美国陶氏有机硅公司 | Use the method and apparatus for carrying out this method of volatile component in the elastomer adsorbent depletion mixture of crosslinking |
| CN110382083A (en) * | 2017-03-14 | 2019-10-25 | 美国陶氏有机硅公司 | Use the method and apparatus for carrying out this method of the organosilicon composition in adsorbent copolymer depletion mixture |
| CN110382083B (en) * | 2017-03-14 | 2022-03-29 | 美国陶氏有机硅公司 | Method for depleting organosilicon components in mixtures using adsorbent copolymers and device for carrying out said method |
| WO2022135944A3 (en) * | 2020-12-21 | 2022-08-18 | IFP Energies Nouvelles | Method for capturing silicon at low hourly space velocity |
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|---|---|
| CN1191328C (en) | 2005-03-02 |
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