CN202379949U - Device for continuous separation and extraction of n-alkanes from naphtha - Google Patents
Device for continuous separation and extraction of n-alkanes from naphtha Download PDFInfo
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- CN202379949U CN202379949U CN2011205036919U CN201120503691U CN202379949U CN 202379949 U CN202379949 U CN 202379949U CN 2011205036919 U CN2011205036919 U CN 2011205036919U CN 201120503691 U CN201120503691 U CN 201120503691U CN 202379949 U CN202379949 U CN 202379949U
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Abstract
A device for continuous separation and extraction of n-alkanes from naphtha is applied to petrochemical engineering for continuous separation and extraction of n-alkanes from naphtha. A material tan is connected with a feeding pump which is connected with a material heater inlet. A material heater outlet is connected with material inlets at the tops of adsorption and desorption columns, including a first adsorption and desorption column and a second adsorption and desorption column connected in parallel. An outlet of a nitrogen heater is connected to nitrogen inlets at the tops of the two adsorption and desorption columns. Two n-alkane outlets of the two adsorption and desorption columns are connected with an n-alkane condenser, an n-alkane storage tank and an n-alkane outlet pump. Non-normal alkane outlets of the two adsorption and desorption columns are connected with a non-normal alkane condenser, a non-normal alkane storage tan and a non-normal alkane outlet pump. The device has the advantage that intermittent production of n-alkanes and non-normal alkanes is changed into continuous production by adding one adsorption and desorption column.
Description
Technical field
The utility model relates to the petrochemical technology field, particularly is raw material with the petroleum naphtha, and separation and Extraction goes out the device of normal paraffin wherein continuously.
Background technology
Developed the octane value of normal paraffin working method raising gasoline in the molecular sieve adsorption separation of lighter gasoline end of the fifties in last century; Process uses the 5A molecular sieve to be sorbent material; With low grade normal paraffin, ammonia, hydrogen or water vapor etc. is desorbing agent. it is good that the stop bracket gasoline that this method is produced has a lead susceptibility; Advantages such as the capability of antidetonance is strong, and environmental pollution is light.At present, use this separation method, with the normal paraffin in the oil product with after non-n-alkane separates, when utilizing non-n-alkane to do the gasoline blend component, the normal paraffin that the development and use desorption comes out out, i.e. desorption oil.In the upgrading process of lightweight direct current gasoline and reforming raffinate oil, desorption oil uses as petrochemical materials and solvent oil.The solvent oil production that China is present, most straight-runs of refinerys that adopt divide oil tech, and sulphur, nitrogen content are high, and aromatic hydrocarbons, ethylenic unsaturation hydrocarbon content are many, cause that the product taste is big, strong toxicity, color be heavy.NPH kind solvent oil be petroleum products through unifining desulfurization, denitrogenation, take off flavor, have good chemicalstability with the dissolving selectivity.
Normal paraffin content is high, and the low desorption oil of aromaticity content is as the cracking of ethylene raw material.Cracking stock is the primary factor that influences the ethene cost, improves product yield and reduction comprehensive energy consumption.Usually, cracking stock accounts for ethene and generates total cost and get more than 70%.In cracking process, purpose products such as the easiest generation ethene of normal paraffin.Therefore, the oil product oil that gets alkane content or select high alkane content in the raising cracking stock can improve ethylene yield as cracking stock, reduces quality pyrolysis gasoline productive rate inferior, reduces the tube coking amount, prolongation on-stream time, economic benefit raising.
The device formation is single in the most oil refining enterprises of China, mainly is made up of atmospheric and vacuum distillation and CCU, lacks catalytic reforming unit, and alkylation, MTBE and isomerization unit are just still less.Therefore China's gasoline blending component is very dull, and the catalytically cracked gasoline component on average accounts for more than 80%, even the dispatch from the factory catalytically cracked gasoline component of gasoline 100% of some enterprise.And external gasoline composition generally is that catalytic cracking and CR gasoline respectively account for about 1/3rd, and one of its excess-three branch is alkylate oil, isomerized oil and MTBE etc.Normal paraffin is the undesirable components in the petroleum products, and the hydroisomerization technology then seems even more important as the means of production high-quality petroleum products.
In addition, desorption oil can increase catalyst activity as hydrogen manufacturing or system ammonia synthesis gas raw material, improves processing power.
C nitrogen 00310122456.7 provides a kind of method of from C5～C6 alkane isomerization product, separating normal paraffin; Earlier the iso-pentane in the raw material is removed, and then it is fed the fractionation by adsorption post, adsorb normal paraffin wherein down at 2.0～4.0MPa, 100～150 ℃, liquid-phase condition; Wait to adsorb saturated after; With the iso-pentane is irrigation, the fractionation by adsorption post is washed, and then be that desorbing agent carries out desorption to the fractionation by adsorption post with the normal paraffin of C7～C9.This method can effectively be separated the normal paraffin in the light hydrocarbon isomerization product, and the consumption of said desorbing agent is few, desorption time short.
CN1715368A discloses a kind of method of from full cut petroleum naphtha, separating normal paraffin; Earlier the aromatic hydrocarbons in the full cut petroleum naphtha is removed from raw material with adsorption method of separation, the normal paraffin that will take off in the full cut petroleum naphtha behind the aromatic hydrocarbons with adsorption method of separation again separates with non-n-alkane.The component that is rich in normal paraffin after the fractionation by adsorption in the naphtha fraction can be used as the charging of steam cracking device; Improve the rare yield of second of steam cracking device; The component that is rich in isoparaffin can be used as the raw material of catalytic reforming unit; Increase reformed gasoline or aromatics yield, the component that is rich in aromatic hydrocarbons then can be used as the charging of coking or reformer.In addition, two kinds of fractionation by adsorption of the utility model have all been selected effective desorbing agent for use, can make the sorbent material effective regeneration of absorption after saturated, utilize again.
The normal paraffin that present molecular sieving extracts in the oil product all is to adopt an adsorption/desorption tower, all is periodical operation therefore.Above-mentioned patent adopts periodical operation to come the normal paraffin in the separation and Extraction oil product.The adsorption operations condition, desorbing agent and desorption manipulation condition are different, and separating resulting is difference to some extent also.
The utility model content
The purpose of the utility model is: the device of normal paraffin in a kind of continuous separation and Extraction petroleum naphtha is provided, under the prerequisite that does not change original basic technology condition, increases an adsorption/desorption tower, reach the quantity-produced purpose.In addition, increase an intermediate oil pump and respective lines, make the intermediate oil of collection can get back to reaction again in the head tank, make full use of raw material resources.
The technical scheme that the utility model adopts is: the device of normal paraffin in the continuous separation and Extraction petroleum naphtha comprises head tank, fresh feed pump, feed heater, nitrogen heater, adsorption/desorption tower, normal paraffin condensing surface, normal paraffin storage tank, normal paraffin outlet pump, non-n-alkane condensing surface, non-n-alkane storage tank, non-n-alkane outlet pump, intermediate oil condensing surface, intermediate oil storage tank and intermediate oil outlet pump.Outlet at head tank connects fresh feed pump through pipeline, and the charging pump outlet connects the inlet of feed heater through pipeline; The outlet of feed heater connects the feed(raw material)inlet of adsorption/desorption top of tower through pipeline; It is characterized in that: described adsorption/desorption tower has the first adsorption/desorption tower and the second adsorption/desorption tower, and the outlet of feed heater connects the feed(raw material)inlet that connects the first adsorption/desorption tower and the second adsorption/desorption top of tower respectively through pipeline; Be connected the outlet of nitrogen heater respectively through pipeline at the nitrogen inlet of the first adsorption/desorption tower and the second adsorption/desorption top of tower;
In the bottom of the first adsorption/desorption tower and the second adsorption/desorption tower three outlets are arranged respectively, i.e. normal paraffin outlet, non-n-alkane outlet and intermediate oil outlet;
The normal paraffin outlet of the first adsorption/desorption tower and the second adsorption/desorption tower has pipeline to be connected the inlet of normal paraffin condensing surface; The outlet of normal paraffin condensing surface has pipeline to connect the inlet of normal paraffin storage tank; The outlet of normal paraffin tank bottom has pipeline to connect the inlet of normal paraffin outlet pump, and the outlet of normal paraffin tank top has pipeline to connect the inlet of normal paraffin condensing surface;
The non-n-alkane outlet of the first adsorption/desorption tower and the second adsorption/desorption tower has pipeline to be connected the inlet of non-n-alkane condensing surface; The outlet of non-n-alkane condensing surface has pipeline to connect the inlet of non-n-alkane storage tank; The outlet of non-n-alkane tank bottom has pipeline to connect the inlet of non-n-alkane outlet pump, and the outlet of non-n-alkane tank top has pipeline to connect the inlet of non-n-alkane condensing surface;
The intermediate oil outlet of the first adsorption/desorption tower and the second adsorption/desorption tower has pipeline to be connected the inlet of intermediate oil condensing surface; The outlet of intermediate oil condensing surface has pipeline to connect the inlet of intermediate oil storage tank; The outlet of intermediate oil tank bottom has pipeline to connect the inlet of intermediate oil outlet pump, and the outlet of intermediate oil tank top has pipeline to connect the inlet of intermediate oil condensing surface; Intermediate oil outlet pump outlet has pipeline to connect the inlet of head tank.
Sketch the technological process of the device of normal paraffin in the continuous separation and Extraction petroleum naphtha.After will vaporizing through well heater from the petroleum naphtha of head tank; From the charging of adsorption/desorption cat head; Adsorption temp is controlled at 250～350 ℃; Adsorption time is 1～2h, does not have non-n-alkane extraction at the bottom of the adsorption/desorption tower of absorption, gets into the non-n-alkane jar after becoming liquid phase through the non-n-alkane condenser condenses.Earlier nitrogen heating back is fed the adsorption/desorption tower with in the tower during desorption, residual petroleum naphtha purges out, and at the bottom of the adsorption/desorption tower, discharges after the intermediate oil condenser condenses gets off to get into the intermediate oil storage tank.After purging totally; Nitrogen is heated to 200～250 ℃; Feed from cat head, desorption time 1～2h desorbs the normal paraffin that is adsorbed in the molecular sieve; Nitrogen is being carried the gasiform normal paraffin secretly and at the bottom of the adsorption/desorption tower, is being discharged entering normal paraffin condensing surface, and condensed liquid normal paraffin is collected in the normal paraffin storage tank.So just realized that molecular sieving extracts normal paraffin in the petroleum naphtha.
In order to reach continuous production normal paraffin and non-n-alkane, adopt the first adsorption/desorption tower to be connected side by side with the second adsorption/desorption tower, be filled with the 5A molecular sieve in the first adsorption/desorption tower and the second adsorption/desorption tower.When the first adsorption/desorption tower was in adsorbed state, the second adsorption/desorption tower carried out the desorb part operation, and the red-tape operati parameter makes it accomplish corresponding section production simultaneously.Through valve and switching pump, when the first adsorption/desorption tower carried out the desorb part operation, the second adsorption/desorption tower adsorbed, by that analogy then.So just can reach the purpose that continuously produces normal paraffin and non-n-alkane.
The beneficial effect of the utility model: the device of normal paraffin in the continuous separation and Extraction petroleum naphtha of the utility model; Through on the basis of original processing unit, increasing an adsorption/desorption tower; And corresponding utility appliance, having reached change batch production normal paraffin and non-n-alkane is continuous production.Because two tower operating parameterss are consistent,, can reach steady production so can not increase the difficulty of producing in the process.Through the switching of two tower production statuses, reach the continuity of production on the whole.The intermediate oil jar that is provided with can be recovered to the petroleum naphtha that is not adsorbed normal paraffin together, and incoming stock jar and raw materials mix make full use of raw material like this, and save energy improves the normal paraffin yield.
Description of drawings
Fig. 1 is the apparatus structure synoptic diagram of normal paraffin in the continuous separation and Extraction petroleum naphtha of the utility model.
Among the figure, 1-head tank, 2-fresh feed pump, 3-feed heater; The 4-nitrogen heater, the 5-first adsorption/desorption tower, the 6-second adsorption/desorption tower, 7-normal paraffin condensing surface; 8-normal paraffin storage tank, 9-normal paraffin outlet pump, 10-non-n-alkane condensing surface, 11-non-n-alkane storage tank; 12-non-n-alkane outlet pump, 13-intermediate oil condensing surface, 14-intermediate oil storage tank, 15-intermediate oil outlet pump.
Embodiment
Embodiment 1: the device with normal paraffin in the continuous separation and Extraction petroleum naphtha is an example, and the utility model is done further explain.
Consult Fig. 1.The device of normal paraffin in the continuous separation and Extraction petroleum naphtha of the utility model comprises head tank 1, fresh feed pump 2, feed heater 3, nitrogen heater 4, adsorption/desorption tower, normal paraffin condensing surface 7, normal paraffin storage tank 8, normal paraffin outlet pump 9, non-n-alkane condensing surface 10, non-n-alkane storage tank 11, non-n-alkane outlet pump 12, intermediate oil condensing surface 13, intermediate oil storage tank 14 and intermediate oil outlet pump 15.
Outlet at head tank 1 connects fresh feed pump 2 through pipeline, and the outlet of fresh feed pump 2 connects the inlet of feed heater 3 through pipeline.The outlet of feed heater 3 connects the feed(raw material)inlet of adsorption/desorption top of tower through pipeline.Described adsorption/desorption tower has the first adsorption/desorption tower 5 and the second adsorption/desorption tower 6, and the outlet of feed heater 3 connects the feed(raw material)inlet that connects the first adsorption/desorption tower 5 and the second adsorption/desorption tower, 6 tops respectively through pipeline.Be connected the outlet of nitrogen heater 4 respectively through pipeline at the first adsorption/desorption tower 5 and the nitrogen inlet at the second adsorption/desorption tower, 6 tops.On the pipeline of the nitrogen inlet at the first adsorption/desorption tower 5 and the second adsorption/desorption tower, 6 tops and feed(raw material)inlet, be connected with a valve respectively.
In the bottom of the first adsorption/desorption tower 5 and the second adsorption/desorption tower 6 three outlets are arranged respectively, i.e. normal paraffin outlet, non-n-alkane outlet and intermediate oil outlet.On the pipeline of normal paraffin outlet, non-n-alkane outlet and intermediate oil outlet, be connected with a valve respectively.
The normal paraffin outlet of the first adsorption/desorption tower 5 and the second adsorption/desorption tower 6 has pipeline to be connected the inlet of normal paraffin condensing surface 7; The outlet of normal paraffin condensing surface 7 has pipeline to connect the inlet of normal paraffin storage tank 8; Normal paraffin storage tank 8 outlet at bottoms have pipeline to connect the inlet of normal paraffin outlet pump 9, and normal paraffin storage tank 8 top exits have pipeline to connect the inlet of normal paraffin condensing surface 7.
The non-n-alkane outlet of the first adsorption/desorption tower 5 and the second adsorption/desorption tower 6 has pipeline to be connected the inlet of non-n-alkane condensing surface 10; The outlet of non-n-alkane condensing surface 10 has pipeline to connect the inlet of non-n-alkane storage tank 11; Non-n-alkane storage tank 11 outlet at bottoms have pipeline to connect the inlet of non-n-alkane outlet pump 12, and non-n-alkane storage tank 11 top exits have pipeline to connect the inlet of non-n-alkane condensing surface 10.
The intermediate oil outlet of the first adsorption/desorption tower 5 and the second adsorption/desorption tower 6 has pipeline to be connected the inlet of intermediate oil condensing surface 13; The outlet of intermediate oil condensing surface 13 has pipeline to connect the inlet of intermediate oil storage tank 14; Intermediate oil storage tank 14 outlet at bottoms have pipeline to connect the inlet of intermediate oil outlet pump 15, and intermediate oil storage tank 14 top exits have pipeline to connect the inlet of intermediate oil condensing surface 13.The outlet of intermediate oil outlet pump 15 has pipeline to connect the inlet of head tank 1.
Claims (1)
1. the device of normal paraffin in the continuous separation and Extraction petroleum naphtha comprises that head tank (1), fresh feed pump (2), feed heater (3), nitrogen heater (4), adsorption/desorption tower, normal paraffin condensing surface (7), normal paraffin storage tank (8), normal paraffin outlet pump (9), non-n-alkane condensing surface (10), non-n-alkane storage tank (11), non-n-alkane outlet pump (12), intermediate oil condensing surface (13), intermediate oil storage tank (14) export pump (15) with intermediate oil; Outlet at head tank (1) connects fresh feed pump (2) through pipeline, and the outlet of fresh feed pump (2) connects the inlet of feed heater (3) through pipeline; The outlet of feed heater (3) connects the feed(raw material)inlet of adsorption/desorption top of tower through pipeline; It is characterized in that: described adsorption/desorption tower has the first adsorption/desorption tower (5) and the second adsorption/desorption tower (6), and the outlet of feed heater (3) connects the feed(raw material)inlet that connects the first adsorption/desorption tower (5) and second adsorption/desorption tower (6) top respectively through pipeline; Be connected the outlet of nitrogen heater (4) respectively through pipeline at the first adsorption/desorption tower (5) and the nitrogen inlet at second adsorption/desorption tower (6) top;
Three outlets are arranged respectively at the bottom at the first adsorption/desorption tower (5) and the second adsorption/desorption tower (6), i.e. normal paraffin outlet, non-n-alkane outlet and intermediate oil outlet;
The normal paraffin outlet of the first adsorption/desorption tower (5) and the second adsorption/desorption tower (6) has pipeline to be connected the inlet of normal paraffin condensing surface (7); The outlet of normal paraffin condensing surface (7) has pipeline to connect the inlet of normal paraffin storage tank (8); Normal paraffin storage tank (8) outlet at bottom has pipeline to connect the inlet of normal paraffin outlet pump (9), and normal paraffin storage tank (8) top exit has pipeline to connect the inlet of normal paraffin condensing surface (7);
The non-n-alkane outlet of the first adsorption/desorption tower (5) and the second adsorption/desorption tower (6) has pipeline to be connected the inlet of non-n-alkane condensing surface (10); The outlet of non-n-alkane condensing surface (10) has pipeline to connect the inlet of non-n-alkane storage tank (11); Non-n-alkane storage tank (11) outlet at bottom has pipeline to connect the inlet of non-n-alkane outlet pump (12), and non-n-alkane storage tank (11) top exit has pipeline to connect the inlet of non-n-alkane condensing surface (10);
The intermediate oil outlet of the first adsorption/desorption tower (5) and the second adsorption/desorption tower (6) has pipeline to be connected the inlet of intermediate oil condensing surface (13); The outlet of intermediate oil condensing surface (13) has pipeline to connect the inlet of intermediate oil storage tank (14); Intermediate oil storage tank (14) outlet at bottom has pipeline to connect the inlet of intermediate oil outlet pump (15), and intermediate oil storage tank (14) top exit has pipeline to connect the inlet of intermediate oil condensing surface (13); The outlet of intermediate oil outlet pump (15) has pipeline to connect the inlet of head tank (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011205036919U CN202379949U (en) | 2011-12-06 | 2011-12-06 | Device for continuous separation and extraction of n-alkanes from naphtha |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011205036919U CN202379949U (en) | 2011-12-06 | 2011-12-06 | Device for continuous separation and extraction of n-alkanes from naphtha |
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| Publication Number | Publication Date |
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| CN202379949U true CN202379949U (en) | 2012-08-15 |
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| CN2011205036919U Expired - Lifetime CN202379949U (en) | 2011-12-06 | 2011-12-06 | Device for continuous separation and extraction of n-alkanes from naphtha |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109731369A (en) * | 2019-02-19 | 2019-05-10 | 安徽国孚凤凰科技有限公司 | A kind of multi-stage absorption extracting II class base oil device of production |
-
2011
- 2011-12-06 CN CN2011205036919U patent/CN202379949U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109731369A (en) * | 2019-02-19 | 2019-05-10 | 安徽国孚凤凰科技有限公司 | A kind of multi-stage absorption extracting II class base oil device of production |
| CN109731369B (en) * | 2019-02-19 | 2024-05-14 | 安徽国孚凤凰科技有限公司 | Device for producing II-type base oil through multistage adsorption extraction |
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| GR01 | Patent grant | ||
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Granted publication date: 20120815 |
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| CX01 | Expiry of patent term |