CN105541540A - Environment-friendly foaming agent and solvent oil co-production device and preparation method thereof - Google Patents
Environment-friendly foaming agent and solvent oil co-production device and preparation method thereof Download PDFInfo
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- CN105541540A CN105541540A CN201610036176.1A CN201610036176A CN105541540A CN 105541540 A CN105541540 A CN 105541540A CN 201610036176 A CN201610036176 A CN 201610036176A CN 105541540 A CN105541540 A CN 105541540A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/18—Solvents
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The invention provides an environment-friendly foaming agent and solvent oil co-production device and a preparation method thereof. According to the technical scheme, the device mainly comprises a hydrogenation reaction system I (1), a hydrogenation reaction system II (2), a solvent oil rectifying tower I (3), a solvent oil rectifying tower II (4), a C5 separation tower (5), a liquefied gas separation tower (6), an isopentane separation tower (7), an n-pentane separation tower (8), a de-heavy tower (9), a solvent oil rectifying tower III (10), an isohexane separation tower (11), an n-hexane extraction tower (12), an extraction reflux tower I (13), a methylcyclopentane extraction tower (14), an extraction reflux tower II (15), a benzene separation tower (16), a C5 hydrogenation feeding pipe (17), a light dydrocarbon feeding pipe (18), a solvent oil hydrogenation feeding pipe (19) and a hexane extraction feeding pipe (20). The device and the preparation method have the following beneficial effects: the technology is simple and practical; the device is low in energy consumption, safe and environment-friendly; the obtained products are stable and reliable in quality, flexible to adjust and high in added value; and the equipment investment and the operational risk are greatly reduced.
Description
Technical field:
The present invention relates to solvent oil technical field, especially a kind of environment-friendly foaming agent and solvent oil combination preparing device and preparation method thereof.
Background technology:
Solvent oil production technology mainly contains extraction fractional distillation, adsorption method of separation, sulfonation method and shortening method both at home and abroad at present.Wherein shortening method is the method be most widely used, shortening method solvent oil is produced and is comprised cut and refining two processes, cut process has following three kinds of approach usually: directly cut by atmospheric tower, corresponding light straight run fraction is cut into suitable narrow fraction again, then will raffinate oil and carry out fractionation and refine.All kinds of SOLVENTS oil distillate generally all needs through refining processing, to improve color and luster, improves stability, removing corrosives and reduction toxicity etc.Conventional process for purification has the refining and hydrofining of alkali cleaning, white scholar etc.Above technology is in application process, due to feedstock property, the know-how restriction of device and auxiliary facility scale of investment and investor, do not realize early stage raw materials pretreatment and later product process for refining required equipment resource optimization prepare, catalyst choice desulfurization, denitrogenation, deoxidation, dechlorination, take off alkene and take off fragrant ability, cause technique short slab, cause unstable product quality, product specification is low, and production cost is high, without market competition advantage.In order to play the integration of each technical process further, improving the quality of products, increasing product yield, in the urgent need to being optimized solvent oil production method, upgrade application new catalyst and energy-efficient equipment.
Summary of the invention
The object of the invention is to overcome above-mentioned deficiency, there is provided and adopt rectifying, cycling extraction and selec-tive hydrogenation process for refining, there is provided alkane product component purity high, product is various, transformation efficiency is high a kind of environment-friendly foaming agent and solvent oil combination preparing device and preparation method thereof, its technical scheme is: connect with liquefied gas knockout tower in hydrogenation reaction system I top, bottom is by head tank and C
5knockout tower, the series connection of solvent oil rectifying tower III top, push up with solvent oil rectifying tower II bottom hydrogenation reaction system II and connect, connect with bottom solvent oil rectifying tower I in top, solvent oil rectifying tower II and C
5knockout tower is connected, and connects at the bottom of tower with at the bottom of weight-removing column, C
5be separated tower top to be connected with bottom hydrogenation reaction system I by head tank, connect with lighter hydrocarbons charging in middle part, connect with solvent oil rectifying tower II in bottom, connect with hydrogenation reaction system I top in the middle part of liquefied gas knockout tower, at the bottom of tower successively with isopentane separation tower, Skellysolve A knockout tower is connected, connect with n-hexane extraction tower in weight-removing column top, middle part respectively with solvent oil rectifying tower II, n-hexane extraction tower is connected, connect with solvent oil rectifying tower III in bottom, solvent oil rectifying tower III pushes up connects with hydrogenation reaction system I through head tank, middle part and weight-removing column, hexane extraction charging is connected, connect with isohexane knockout tower in bottom, connect with solvent oil rectifying tower III in the middle part of isohexane knockout tower, connect with in the middle part of weight-removing column in bottom, connect with bottom extract return method tower I in n-hexane extraction tower top, connect with in the middle part of extract return method tower I in bottom, connect with weight-removing column top in bottom, connect with in the middle part of methylcyclopentane extraction tower in extract return method tower I top, connect with bottom extract return method tower II in methylcyclopentane extraction tower top, connect with extract return method tower II bottom in bottom, connect with in the middle part of benzene knockout tower in extract return method tower II top, hexane extraction feed-pipe connects solvent oil rectifying tower III, C
5hydrogenation feed-pipe connects hydrogenation reaction system I, and lighter hydrocarbons feed-pipe connects C
5knockout tower, solvent oil hydrogenation feed-pipe connects hydrogenation reaction system II.
Solvent oil rectifying tower I overhead product is 6# solvent oil, and the bottomsstream is 120# solvent oil; Solvent oil rectifying tower II overhead product is 6#, 120# oil miscible solvent compound; C
5knockout tower overhead product is C
5component; Liquefied gas knockout tower overhead product is liquefied gas; Isopentane separation column overhead overhead product is iso-pentane; Skellysolve A knockout tower overhead product is Skellysolve A; Weight-removing column overhead product is 140# solvent oil or n-hexane extraction tower required extraction material, and the bottomsstream is for cutting excess oil, and solvent oil rectifying tower III overhead product is 200# solvent oil or C
5component, the bottomsstream is for cutting excess oil; Isohexane knockout tower overhead product is isohexane; N-hexane extraction column overhead overhead product is normal hexane; Methylcyclopentane extraction tower overhead product is methylcyclopentane; Benzene knockout tower overhead product is benzene, and the bottomsstream is xylol.
Preparation method comprises the steps:
(1), first carry out raw materials pretreatment, according to feedstock property, selective gist pickling, alkali cleaning, dewatering type carry out raw materials pretreatment, reduce moisture, sulphur, chlorine, nitrogen impurity content in raw material;
(2), raw material through distillation or extraction after, by generate solvent oil and C
5mixture carries out hydrofining respectively, remove the sulphur in product, nitrogen, oxygen, chlorine, aromatic hydrocarbons and alkene, again through rectifying, cut out environmental protection, high pure naphtha and whipping agent product, again can carry out that alkali cleaning is refining or to carry out dehydration with Calcium Chloride Powder Anhydrous etc. refining before product export for specific demand, improve product purity further;
(3), Combination application hydrogenation scavenging agent, catalyzer, ensure desulfurization, denitrogenation, deoxidation, dechlorination, de-alkene, Tuo Fang and decontamination effect improving, hydrogenation system outlets products index is not less than following requirement: total sulfur: < lppm, bromine index: < 20mgBr/l00g, Cl < 1ppm, benzene content < 0.01%;
(4), hydrogenated oil and C
5mixture cools laggard cold high pressure separator through heat exchange, after gas-liquid separation, enters rectifying tower rectifying through surge tank, through compressor compresses after cold high pressure separator recycle hydrogen out mixes with hydrogen make-up, send to mix with raw material and recycles;
(5), rectifying tower tower bottom reboiler thermal source adopts 1.0Mpa, 200 DEG C of steam, overhead condenser, overhead product water cooler heat-eliminating medium adopt recirculated cooling water, wherein weight-removing column top temperature 96.7 DEG C, end temperature 150 DEG C, tower top pressure 0.22MPa, tower bottom pressure 0.27MPa, removes the heavy constituent of cut >=96 DEG C;
(6), be provided with revivifier at the bottom of extract return method tower tower, effectively remove extraction agent impurity, save Solvent quantity,
For improving heat exchange efficiency and the degree of depth, effectively reduce extraction agent backflow pressure drop, extract return method column overhead condenser, overhead product water cooler adopt the reverse-flow steel alloy interchanger of corrugated tube, and heat-eliminating medium adopts ethylene glycol.
Beneficial effect of the present invention: the present invention adopts rectifying, cycling extraction and selec-tive hydrogenation process for refining, supporting hydrogen production units by carbinol and two groups of hydrogenation reaction systems, apply novel high-selectivity catalyst, optimize reaction velocity and related process operating parameters, intensified response activity, the selec-tive hydrogenation treating process of reactant is after pretreatment completed under lower temperature, pressure, remove the impurity such as the sulphur in raw material, nitrogen, oxygen, chlorine, alkene and aromatic hydrocarbons, some olefin generates alkane through addition reaction, increases alkane yield.Gained C
5following light constituent can be sold by high-purity monomer alkane, and Skellysolve A, iso-pentane product purity reach 99.9%, can prepare environment-friendly foaming agent in any proportion, and all the other heavy constituents produce 6#, 120#, 140#, 200# equal solvent oil.The method of the invention, catalyzer operational condition is relatively gentle, desulfurization, denitrogenation, deoxidation, dechlorination, de-alkene and de-fragrant Be very effective, features simple and practical process, plant energy consumption is low, safety and environmental protection, and the adjustment of stable and reliable product quality, product flexibly, added value of product is high, greatly reduces facility investment and operational risk.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Embodiment
As shown in Figure 1, a kind of environment-friendly foaming agent and solvent oil combination preparing device and preparation method thereof, primarily of hydrogenation reaction system I 1, hydrogenation reaction system II 2, solvent oil rectifying tower I 3, solvent oil rectifying tower II 4, C
5knockout tower 5, liquefied gas knockout tower 6, isopentane separation tower 7, Skellysolve A knockout tower 8, weight-removing column 9, solvent oil rectifying tower III 10, isohexane knockout tower 11, n-hexane extraction tower 12, extract return method tower I 13, methylcyclopentane extraction tower 14, with extract return method tower II 15, benzene knockout tower 16, C
5hydrogenation feed-pipe 17, lighter hydrocarbons feed-pipe 18, solvent oil hydrogenation feed-pipe 19 and hexane extraction feed-pipe 20 are formed, connect with liquefied gas knockout tower 6 in hydrogenation reaction system I 1 top, bottom is by head tank and C
5knockout tower 5, the series connection of solvent oil rectifying tower III 10 top, push up with solvent oil rectifying tower II 4 bottom hydrogenation reaction system II 2 and connect, connect with bottom solvent oil rectifying tower I 3 in top, solvent oil rectifying tower II 4 and C
5knockout tower 5 is connected, and connects at the bottom of tower with weight-removing column 9 end, C
5knockout tower 5 pushes up is connected with bottom hydrogenation reaction system I 1 by head tank, connect with lighter hydrocarbons charging 18 in middle part, connect with solvent oil rectifying tower II 4 in bottom, connect with hydrogenation reaction system I 1 top in the middle part of liquefied gas knockout tower 6, at the bottom of tower successively with isopentane separation tower 7, Skellysolve A knockout tower 8 is connected, connect with n-hexane extraction tower 12 in weight-removing column 9 top, middle part respectively with solvent oil rectifying tower II 4, n-hexane extraction tower 12 is connected, connect with solvent oil rectifying tower III 10 in bottom, connect with hydrogenation reaction system I 1 through head tank in solvent oil rectifying tower III 10 top, middle part and weight-removing column 9, hexane extraction charging 20 is connected, connect with isohexane knockout tower 11 in bottom, connect with solvent oil rectifying tower III 10 in the middle part of isohexane knockout tower 11, connect with in the middle part of weight-removing column 9 in bottom, connect with bottom extract return method tower I 13 in n-hexane extraction tower 12 top, connect with in the middle part of extract return method tower I 13 in bottom, connect with weight-removing column 9 top in bottom, connect with in the middle part of methylcyclopentane extraction tower 14 in extract return method tower I 13 top, connect with bottom extract return method tower II 15 in methylcyclopentane extraction tower 14 top, connect with extract return method tower II 15 bottom in bottom, connect with in the middle part of benzene knockout tower 16 in extract return method tower II 15 top, hexane extraction feed-pipe 20 connects solvent oil rectifying tower III 10, C
5hydrogenation feed-pipe 17 connects hydrogenation reaction system I 1, and lighter hydrocarbons feed-pipe 18 connects C
5knockout tower 5, solvent oil hydrogenation feed-pipe 19 connects hydrogenation reaction system II 2.
Present invention process flow process: first carry out raw materials pretreatment.According to feedstock property, the modes such as selective gist pickling, alkali cleaning, dehydration carry out raw materials pretreatment, reduce the foreign matter content such as moisture, sulphur, chlorine, nitrogen in raw material, alleviate equipment corrosion, extending catalyst work-ing life.
Raw material through distillation or extraction after, by generate solvent oil and C
5mixture carries out hydrofining respectively, removes the sulphur in product, nitrogen, oxygen, chlorine, aromatic hydrocarbons and alkene, then through rectifying, cuts out environmental protection, high pure naphtha and whipping agent product.Again can carry out that alkali cleaning is refining or to carry out dehydration with Calcium Chloride Powder Anhydrous etc. refining before product export for specific demand, improve product purity further.
Combination application hydrogenation scavenging agent, catalyzer, ensure desulfurization, denitrogenation, deoxidation, dechlorination, de-alkene, Tuo Fang and decontamination effect improving.Hydrogenation system outlets products index is not less than following requirement: total sulfur: < lppm; Bromine index: < 20mgBr/l00g; Cl < 1ppm; Benzene content < 0.01%.
Application is with MgO, Al
3o2, CaO and promotor etc. are the dechlorinating agent of major ingredient, air speed: 1000 ~ 3000h
-1(gas), 0.5 ~ 3h
-1(liquid); Temperature: 200 ~ 400 DEG C; Pressure: normal pressure ~ 8.0Mpa, to solvent oil and C
5mixture carries out dechlorination desulfurization.
Apply and add with active ZnO the medium temperature desulfurating agent that promotor is major ingredient, operational condition: air speed: 500 ~ 3000h
-1(gas), 0.5 ~ 3h
-1(liquid); Temperature: 200 ~ 400 DEG C; Pressure: normal pressure ~ 30.0Mpa, desolvation oil and C
5sulfide in mixture.
Application is with Co, Mo, Ni, Wo, Al
2o
3deng the Hydrobon catalyst for major ingredient, operational condition: air speed: 1-6h
-1(liquid); Temperature: 200-400 DEG C; Pressure: 0.1-3.0Mpa; Hydrogen to oil volume ratio:>=100, by solvent oil and C
5organic sulfide hydrocracking in mixture is H
2s, olefins hydrogenation and micro amount of oxygen remove.
Application is with Ni, Pt, Pd, Al
2o
3deng the hydrogenation dearomatization catalyst for major ingredient, operational condition: air speed: 1-3h
-1(liquid); Temperature: 120-220 DEG C; Pressure: 0.1-3.0Mpa; Hydrogen to oil volume ratio:>=100, by solvent oil and C
5aromatic substance hydrocracking in mixture is corresponding naphthenic hydrocarbon, reaches product and takes off fragrant object.
Application is with Ni, Mo, Co, Al
20
3and the hydrogenation that auxiliary agent etc. is major ingredient takes off diolefin catalyzer, operational condition: air speed: 1-3h
-1(liquid); Temperature: 120-220 DEG C; Pressure: 0.1-3.0Mpa; Hydrogen to oil volume ratio:>=100, by solvent oil and C
5double bond hydrogenation of olefins in mixture is converted into corresponding paraffins, reaches product deolefination object.
Hydrogenated oil and C
5mixture cools laggard cold high pressure separator through heat exchange, after gas-liquid separation, enters rectifying tower rectifying through surge tank.Through compressor compresses after cold high pressure separator recycle hydrogen out mixes with hydrogen make-up, send to mix with raw material and recycle.
Rectifying tower tower bottom reboiler thermal source adopts 1.0Mpa, 200 DEG C of steam, and overhead condenser, overhead product water cooler heat-eliminating medium adopt recirculated cooling water.Wherein weight-removing column top temperature 96.7 DEG C, end temperature 150 DEG C, tower top pressure 0.22MPa, tower bottom pressure 0.27MPa, removes the heavy constituent of cut >=96 DEG C.
Be provided with high efficiency regenerator at the bottom of extract return method tower tower, effectively remove extraction agent impurity, save Solvent quantity, extend service life of extractant.
For improving heat exchange efficiency and the degree of depth, effectively reduce extraction agent backflow pressure drop, extract return method column overhead condenser, overhead product water cooler adopt the reverse-flow steel alloy interchanger of corrugated tube, and heat-eliminating medium adopts ethylene glycol.
The present invention adopts rectifying, cycling extraction and selec-tive hydrogenation process for refining, supporting hydrogen production units by carbinol and two groups of hydrogenation reaction systems, apply novel high-selectivity catalyst, optimize reaction velocity and related process operating parameters, intensified response activity, completes the selec-tive hydrogenation treating process of reactant after pretreatment, removes the impurity such as the sulphur in raw material, nitrogen, oxygen, chlorine, alkene and aromatic hydrocarbons under lower temperature, pressure, some olefin generates alkane through addition reaction, increases alkane yield.Gained C
5following light constituent can be sold by high-purity monomer alkane, and Skellysolve A, iso-pentane product purity reach 99.9%, can prepare environment-friendly foaming agent in any proportion, and all the other heavy constituents produce 6#, 120#, 140#, 200# equal solvent oil.The method of the invention, catalyzer operational condition is relatively gentle, desulfurization, denitrogenation, deoxidation, dechlorination, de-alkene and de-fragrant Be very effective, features simple and practical process, plant energy consumption is low, and the adjustment of stable and reliable product quality, product is flexibly, added value of product is high, greatly reduces facility investment and operational risk.
The principle of extraction utilizes the difference of compound solubleness or partition ratio in the solvent of two kinds immiscible (or slightly solubles), and compound is transferred to another solvent in a kind of solvent.Through repeated multiple times extraction transfer, the compound of the overwhelming majority is extracted.The operation of extracting rectifying packing tower, the pressure reduction of tower controls very important, and pressure reduction one changes, and is easy to cause liquid flooding.Cause component defective.In addition, the selection of solvent is very important, keeps a close eye on solvent and bubbles, otherwise solvent foaming also causes liquid flooding.
Lighter hydrocarbons feeding process flow process:
Material in lighter hydrocarbons feed-pipe 18 is through C
5the rectifying cutting successively of knockout tower 5, solvent oil rectifying tower II 4, weight-removing column 9, solvent oil rectifying tower III 10, each rectifying tower overhead product is as follows: C
5knockout tower 5 overhead product is through C
5head tank enters hydrogenation reaction system I 1; Solvent oil rectifying tower II 4 overhead product enters hydrogenation reaction system II 2 through surge tank; Weight-removing column 9 overhead product is 140# solvent oil; Solvent oil rectifying tower III 10 overhead product is 200# solvent oil, and tower undercutting excess oil enters hexane extraction charging.
Hexane extraction feeding process flow process:
Material in hexane extraction feed-pipe 20 is successively through solvent oil rectifying tower III 10, isohexane knockout tower 11, weight-removing column 9, n-hexane extraction tower 12, extract return method tower I 13, methylcyclopentane extraction tower 14, extract return method tower II 15, benzene knockout tower 16 rectifying, extraction, rectifying again, each tower overhead product is as follows: solvent oil rectifying tower III 10 overhead product is through C
5head tank enters hydrogenation reaction system I 1, and the bottomsstream enters isohexane knockout tower 11; Isohexane knockout tower 11 overhead product is isohexane, and the bottomsstream enters weight-removing column 9; Weight-removing column 9 overhead product enters n-hexane extraction tower 12, and the bottomsstream enters light hydrocarbon feedstocks tank freshening; N-hexane extraction tower 12 overhead product is normal hexane, and the bottomsstream enters extract return method tower I 13; Extract return method tower I 13 overhead product enters methylcyclopentane extraction tower 14, and the bottomsstream returns n-hexane extraction tower 12; Methylcyclopentane extraction tower 14 overhead product is methylcyclopentane, and the bottomsstream enters extract return method tower II 15; Extract return method tower II 15 overhead product enters benzene knockout tower 16, and the bottomsstream returns methylcyclopentane extraction tower 14; Benzene knockout tower 16 overhead product is benzene, and the bottomsstream is xylol.
C
5hydrogenation feeding process flow:
In this technical process, hydrogenation reaction system I 1, liquefied gas knockout tower 6, isopentane separation tower 7, Skellysolve A knockout tower 8 are connected successively, raw material is after hydrogenation reaction system I 1 reaction is refining, rectifying tower rectifying is entered: enter liquefied gas knockout tower 6 through high score, liquefied gas knockout tower 6 overhead product is liquefied gas light constituent, and the bottomsstream enters isopentane separation tower 7; Isopentane separation tower 7 overhead product is iso-pentane, and the bottomsstream enters Skellysolve A knockout tower 8; Skellysolve A knockout tower 8 overhead product is Skellysolve A, and overhead product is thick pentamethylene.
Solvent oil hydrogenation feeding process flow process:
Hydrogenation reaction system II 2 is connected with solvent oil rectifying tower I 3.Material in solvent oil hydrogenation feed-pipe 19 is after hydrogenation reaction system II 2 reaction is refining, and enter solvent oil rectifying tower I 3 rectifying through high score: overhead product is 6# solvent oil, the bottomsstream is 120# solvent oil.
Again can carry out that alkali cleaning is refining or to carry out dehydration with Calcium Chloride Powder Anhydrous etc. refining before product export for specific demand, improve product purity further.
The monomer alkane produced is many, and purity is high, unsaturated hydrocarbons content≤0.01%, sulphur content≤1PPM, carbon five content≤0.0005%, and alkane purity is more than 99.9%; Produce high-purity pentane can according to " pentane foaming agent (GB/T22053-2008) " standard preparation all model pentane foaming agents product; Produce 6# solvent oil and meet " GB16629-19966 solvent for extraction " standard-required; Produce 120# solvent oil and meet " SH0004-90 " requirement.
Claims (3)
1. an environment-friendly foaming agent and solvent oil combination preparing device and preparation method thereof, is characterized in that: connect with liquefied gas knockout tower (6) in hydrogenation reaction system I (1) top, bottom is by head tank and C
5knockout tower (5), the series connection of solvent oil rectifying tower III (10) top, hydrogenation reaction system II (2) bottom is pushed up with solvent oil rectifying tower II (4) and is connected, and connect with solvent oil rectifying tower I (3) bottom in top, solvent oil rectifying tower II (4) and C
5knockout tower (5) is connected, and connects at the bottom of tower with weight-removing column (9) end, C
5connected with hydrogenation reaction system I (1) bottom by head tank in knockout tower (5) top, connect with lighter hydrocarbons charging (18) in middle part, connect with solvent oil rectifying tower II (4) in bottom, connect with hydrogenation reaction system I (1) top in liquefied gas knockout tower (6) middle part, at the bottom of tower successively with isopentane separation tower (7), Skellysolve A knockout tower (8) is connected, connect with n-hexane extraction tower (12) in weight-removing column (9) top, middle part respectively with solvent oil rectifying tower II (4), n-hexane extraction tower (12) is connected, connect with solvent oil rectifying tower III (10) in bottom, connect with hydrogenation reaction system I (1) through head tank in solvent oil rectifying tower III (10) top, middle part and weight-removing column (9), hexane extraction charging (20) is connected, connect with isohexane knockout tower (11) in bottom, connect with solvent oil rectifying tower III (10) in isohexane knockout tower (11) middle part, connect with weight-removing column (9) middle part in bottom, connect with extract return method tower I (13) bottom in n-hexane extraction tower (12) top, connect with extract return method tower I (13) middle part in bottom, connect with weight-removing column (9) top in bottom, connect with methylcyclopentane extraction tower (14) middle part in extract return method tower I (13) top, connect with extract return method tower II (15) bottom in methylcyclopentane extraction tower (14) top, connect with extract return method tower II (15) bottom in bottom, connect with benzene knockout tower (16) middle part in extract return method tower II (15) top, hexane extraction feed-pipe (20) connects solvent oil rectifying tower III (10), C
5hydrogenation feed-pipe (17) connects hydrogenation reaction system I (1), and lighter hydrocarbons feed-pipe (18) connects C
5knockout tower (5), solvent oil hydrogenation feed-pipe (19) connects hydrogenation reaction system II (2).
2. a kind of environment-friendly foaming agent according to claim 1 and solvent oil combination preparing device and preparation method thereof, is characterized in that: described solvent oil rectifying tower I (3) overhead product is 6# solvent oil, and the bottomsstream is 120# solvent oil; Described solvent oil rectifying tower II (4) overhead product is 6#, 120# oil miscible solvent compound; Described C
5knockout tower (5) overhead product is C
5component; Described liquefied gas knockout tower (6) overhead product is liquefied gas; Described isopentane separation tower (7) overhead product is iso-pentane; Described Skellysolve A knockout tower (8) overhead product is Skellysolve A; Described weight-removing column (9) overhead product is 140# solvent oil or n-hexane extraction tower (12) required extraction material, and the bottomsstream is for cutting excess oil, and described solvent oil rectifying tower III (10) overhead product is 200# solvent oil or C
5component, the bottomsstream is for cutting excess oil; Described isohexane knockout tower (11) overhead product is isohexane; Described n-hexane extraction tower (12) overhead product is normal hexane; Described methylcyclopentane extraction tower (14) overhead product is methylcyclopentane; Described benzene knockout tower (16) overhead product is benzene, and the bottomsstream is xylol.
3. a kind of environment-friendly foaming agent and solvent oil combination preparing device and preparation method thereof according to right 1 or 2, is characterized in that: its preparation method comprises the steps:
(1), first carry out raw materials pretreatment, according to feedstock property, selective gist pickling, alkali cleaning, dewatering type carry out raw materials pretreatment, reduce moisture, sulphur, chlorine, nitrogen impurity content in raw material;
(2), raw material through distillation or extraction after, by generate solvent oil and C
5mixture carries out hydrofining respectively, remove the sulphur in product, nitrogen, oxygen, chlorine, aromatic hydrocarbons and alkene, again through rectifying, cut out environmental protection, high pure naphtha and whipping agent product, again can carry out that alkali cleaning is refining or to carry out dehydration with Calcium Chloride Powder Anhydrous etc. refining before product export for specific demand, improve product purity further;
(3), Combination application hydrogenation scavenging agent, catalyzer, ensure desulfurization, denitrogenation, deoxidation, dechlorination, de-alkene, Tuo Fang and decontamination effect improving, hydrogenation system outlets products index is not less than following requirement: total sulfur: < lppm, bromine index: < 20mgBr/l00g, Cl < 1ppm, benzene content < 0.01%;
(4), hydrogenated oil and C
5mixture cools laggard cold high pressure separator through heat exchange, after gas-liquid separation, enters rectifying tower rectifying through surge tank, through compressor compresses after cold high pressure separator recycle hydrogen out mixes with hydrogen make-up, send to mix with raw material and recycles;
(5), rectifying tower tower bottom reboiler thermal source adopts 1.0Mpa, 200 DEG C of steam, overhead condenser, overhead product water cooler heat-eliminating medium adopt recirculated cooling water, wherein weight-removing column top temperature 96.7 DEG C, end temperature 150 DEG C, tower top pressure 0.22MPa, tower bottom pressure 0.27MPa, removes the heavy constituent of cut >=96 DEG C;
(6), be provided with revivifier at the bottom of extract return method tower tower, effectively remove extraction agent impurity, save Solvent quantity,
For improving heat exchange efficiency and the degree of depth, effectively reduce extraction agent backflow pressure drop, extract return method column overhead condenser, overhead product water cooler adopt the reverse-flow steel alloy interchanger of corrugated tube, and heat-eliminating medium adopts ethylene glycol.
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| CN107573205A (en) * | 2017-10-27 | 2018-01-12 | 濮阳市联众兴业化工有限公司 | One kind is without naphthalene nucleus pentane production method |
| CN109181766A (en) * | 2018-09-13 | 2019-01-11 | 大庆亿鑫化工股份有限公司 | A kind of modified light aromatic hydrocarbons hydrogenation plant and its operating method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105950213A (en) * | 2016-06-30 | 2016-09-21 | 东营市俊源石油技术开发有限公司 | Environment-friendly solvent and partial monomer alkane production device and use method thereof |
| CN107573205A (en) * | 2017-10-27 | 2018-01-12 | 濮阳市联众兴业化工有限公司 | One kind is without naphthalene nucleus pentane production method |
| CN109181766A (en) * | 2018-09-13 | 2019-01-11 | 大庆亿鑫化工股份有限公司 | A kind of modified light aromatic hydrocarbons hydrogenation plant and its operating method |
| CN110105921A (en) * | 2019-04-28 | 2019-08-09 | 东营市俊源石油技术开发有限公司 | A kind of tasteless environment-friendly aerial fog propellant production equipment and production method |
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| WO2023125044A1 (en) * | 2021-12-31 | 2023-07-06 | 中国石油天然气股份有限公司 | Method and system for producing solvent oil from raffinate oil |
| CN114653319A (en) * | 2022-03-31 | 2022-06-24 | 濮阳市联众兴业化工有限公司 | Device for producing pentane foaming agent and using method |
| CN114653319B (en) * | 2022-03-31 | 2023-12-22 | 濮阳市联众兴业化工有限公司 | Device for producing pentane foaming agent and use method |
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