CN111471486A - Isoparaffin solvent oil composition prepared from coal indirect liquefied product serving as raw material - Google Patents
Isoparaffin solvent oil composition prepared from coal indirect liquefied product serving as raw material Download PDFInfo
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- CN111471486A CN111471486A CN201910060902.7A CN201910060902A CN111471486A CN 111471486 A CN111471486 A CN 111471486A CN 201910060902 A CN201910060902 A CN 201910060902A CN 111471486 A CN111471486 A CN 111471486A
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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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- 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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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the field of fine chemicals, in particular to isoparaffin solvent oil. The technical scheme is that the isoparaffin solvent oil composition is prepared by taking indirect coal liquefaction products as raw materials, and is characterized in that the raw materials are subjected to 5A molecular sieve adsorption, rectification and cutting processes to obtain the isoparaffin, the raw materials are obtained by blending a first indirect coal liquefaction Fischer-Tropsch product and a second indirect coal liquefaction Fischer-Tropsch product according to a certain volume ratio, the weight ratio of normal paraffins to isoparaffins is (0.8-1.1) to 1, and the flash point of the prepared isoparaffin solvent oil composition is 45-61 ℃. The isoparaffin solvent oil has the purity of more than 96 percent, basically does not contain cycloparaffin and arene, has no peculiar smell, narrow distillation range, no toxicity and no color, and is particularly suitable for dry cleaning of clothes and metal cleaning solvent oil.
Description
Technical Field
The invention relates to the field of fine chemicals, in particular to isoparaffin solvent oil.
Background
The traditional solvent oil preparation mostly adopts petroleum hydrocarbon raw materials, and due to the existence of impurities such as S, N and the like in the petroleum raw materials and higher aromatic hydrocarbon content, the technical requirements for producing the low aromatic ring environment-friendly solvent oil are higher, the process flow is complex, and the cost is high, so that the domestic solvent oil production still mainly uses common solvent oil with higher aromatic hydrocarbon content and poor environment-friendly performance, the complex group composition also leads to the complex process flow for producing the normal alkane solvent oil by using the petroleum as the raw materials, the environmental awareness of people is gradually enhanced along with the high-speed development of scientific technology, the requirements for the quality of the solvent oil products are higher and higher, and the environment-friendly solvent oil is required to have low aromatic hydrocarbon content, low sulfur content, low nitrogen content, no toxicity, no odor, no color and strong stability.
The isoparaffin solvent oil has the characteristics of low condensation point, small smell, low toxicity, good stability, higher dissolving capacity than normal paraffin and the like, and is widely used for printing and dyeing diluents, printing ink solvents, metal processing cleaning agents, anti-rust oil, odorless sprays, paint organosol formulas, high-grade clothes dry-cleaning oil, peroxy organic compound carriers, washing daily chemical products and the like. The application field of isoparaffin solvent oil can be generally determined by flash point, for example, isoparaffin with flash point more than 45 ℃ and less than 61 ℃ is mainly used for dry cleaning of clothes and cleaning of metals, isoparaffin with flash point more than 61 ℃ is mainly used for metal processing and coating, isoparaffin with flash point more than 80 ℃ is mainly used for processing aluminum plate and aluminum foil and aerosol insecticide, and isoparaffin with flash point more than 95 ℃ is mainly used for ink solvent.
Chinese patent CN107400535A discloses a method for producing isoparaffin solvent oil from Fischer-Tropsch synthetic naphtha and isoparaffin solvent oil, wherein the Fischer-Tropsch synthetic naphtha is used as a raw material, the Fischer-Tropsch synthetic naphtha is subjected to alcohol halogenation, polymerization and hydrogenation in turn, and specific polymerization conditions are preferably controlled to obtain more dimerization products, so that isoparaffin solvent oil with obviously higher yield and isoparaffin purity can be obtained, the problem of how to process the Fischer-Tropsch synthetic naphtha to obtain isoparaffin solvent oil with high isoparaffin content is solved, the isoparaffin content in the obtained isoparaffin solvent oil is more than 98 wt%, the oxygen content of the isoparaffin solvent oil is less than 0.1 wt%, and the aromatic hydrocarbon content is less than 0.05 vol%. As the selected raw material is Fischer-Tropsch synthesis naphtha containing olefin, organic oxygen-containing compound and more alcohol, and the process is catalytic hydrogenation, the finally obtained isoparaffin solvent oil cannot contain more impurities, so that the quality of the solvent oil is influenced.
Chinese patent CN104910960A discloses a method for producing normal paraffin solvent oil from Fischer-Tropsch synthetic oil, and provides a method for producing a plurality of normal paraffin solvent oil products through hydrofining and multi-step rectification separation, wherein the normal paraffin content in the products is about 88 weight percent, and the preparation of isoparaffin solvent oil is not involved.
Chinese patent CN108102694A (published 6.1.2018) discloses a reprocessing system and method of Fischer-Tropsch synthesis diesel fraction, which can obtain a mixture of C10-C14 normal paraffins and a mixture of C10-C14 isoparaffins through different fractionating towers, and does not obtain a specific isoparaffin solvent oil composition with a flash point of more than 45 ℃ and less than 62 ℃.
The Fischer-Tropsch synthesis product typically contains small amounts of naphthenes, for example less than 10% of naphthenes containing from 9 to 20 carbon atoms in the Fischer-Tropsch synthesis oil disclosed in CN 105505347A; CN106255740A discloses a Fischer-Tropsch derived gasoil containing in the range of 0-2 wt% naphthenes.
At present, the important problem faced by China in the field of isoparaffin solvent oil for dry cleaning of clothes and metal cleaning is that the solvent oil has a certain smell and is limited in market application due to low purity, naphthenic hydrocarbon, aromatic hydrocarbon, S, N and the like. The NemengGueita group is taken as one of leading enterprises in the coal indirect liquefaction oil production industry in China, the coal oil product is taken as a raw material, and a high-purity specific isoparaffin solvent oil for dry cleaning of clothes and metal cleaning is obtained through a fine cutting process, so that the long-standing technical problem in the fields of dry cleaning of clothes and metal cleaning solvent oil is solved.
Technical scheme
The invention aims to solve the technical problem of batch production of the clothing dry-cleaning solvent oil and the metal cleaning solvent oil which are high in purity, odorless, free of cycloparaffin and free of aromatic hydrocarbon.
The technical scheme of the invention is as follows:
the isoparaffin solvent oil composition prepared by taking coal indirect liquefied product as raw material is characterized in that the raw material is subjected to 5A molecular sieve adsorption, rectification and cutting processes to obtain isoparaffin, and the raw material source is that a first coal indirect liquefied Fischer-Tropsch product and a second coal indirect liquefied Fischer-Tropsch product are blended according to a certain volume ratio, so that the weight ratio of normal paraffin to isoparaffin is (0.8-1.1) to 1, and the flash point is 45-61 ℃.
The content of normal paraffin in the first Fischer-Tropsch product indirectly liquefied by coal is more than 90%, wherein the normal paraffin of C9-C18 accounts for more than 96% of the total mass of the normal paraffin, and the content of isoparaffin in the second Fischer-Tropsch product indirectly liquefied by coal is more than 85%, wherein the isoparaffin of C9-C20 accounts for more than 96% of the total mass of the isoparaffin.
The isoparaffin solvent oil composition has a purity of greater than 96%.
The isoparaffin solvent oil composition has a purity of greater than 97%.
The rectification cutting process comprises an isoparaffin separation tower, wherein the pressure at the top of the isoparaffin separation tower is 0.08-0.11MPa, the pressure at the bottom of the isoparaffin separation tower is 0.12-0.15MPa, the temperature at the top of the tower is 198-290 ℃, and the temperature at the bottom of the tower is 270-290 ℃.
The isoparaffin solvent oil composition is 2-methylnonane: 47.9%, isomeric C11: 50.5%, isomeric C12: 0.5%, normal C9-C11: 0.1%, and the distillation range is 170-.
The isoparaffin is free of cycloparaffins and has an aromatic content of less than 50 ppm.
In the raw materials, C5-C9 normal paraffin, C5-C9 isoalkane is (2-5) to 1, C10-C13 normal paraffin, C10-C13 isoalkane is (0.8-1) to 1, C14-C16 normal paraffin, C14-C16 isoalkane is (1-1.2) to 1, C17+ normal paraffin, C17+ isoalkane is (1-1.2) to 1.
And the first Fischer-Tropsch product and the second Fischer-Tropsch product of the coal indirect liquefaction do not contain naphthenes, nitrogen and sulfur.
The beneficial technical effects obtained by the invention are as follows:
the isoparaffin solvent oil provided by the invention has high purity of more than 96%, basically does not contain cycloalkane and arene, has no peculiar smell, has narrow distillation range, is nontoxic and colorless, and is particularly suitable for dry cleaning of clothes and metal cleaning solvent oil.
Drawings
FIG. 1 is a flow chart of the process for producing isoparaffin according to the present invention.
Detailed Description
The present invention will be described in detail below with reference to specific embodiments and the accompanying drawings.
The examples described herein are specific embodiments of the present invention, are intended to be illustrative and exemplary in nature, and are not to be construed as limiting the scope of the invention. In addition to the embodiments described herein, those skilled in the art will be able to employ other technical solutions which are obvious based on the disclosure of the claims and the specification of the present application, and these technical solutions include technical solutions which make any obvious replacement or modification for the embodiments described herein.
Example 1
The Fischer-Tropsch crude liquid wax of the coal-based Fischer-Tropsch synthesis liquefied oil process of the inner Mongolia Guyitai chemical engineering project of 120 ten thousand tons per year coal chemical engineering project is used as a raw material of the project, and the raw material does not contain cyclane.
After the materials enter a feeding buffer tank, the materials enter a lightness-removing tower after being boosted by a pump and heat-exchanged by hot materials, and the tower bottom components of the lightness-removing tower enter a weight-removing tower after being conveyed by a bottom pump of the lightness-removing tower; the light component removal tower preferably adopts plate-type rectification, the pressure at the top of the tower is 0.01-0.05 Mpa, the pressure at the bottom of the tower is 0.02-0.06 Mpa, the temperature at the top of the tower is 155-165 ℃, and the temperature at the bottom of the tower is 210-230 ℃.
After heat exchange is carried out between the tower top components of the de-heavy tower and the cold materials, the tower top components enter a reflux tank, a part of the tower top components is boosted by a pump and returned to the rectifying tower as reflux, and a part of the tower top components is used as a raw material for dewaxing the molecular sieve and enters an adsorption tower after heat exchange; the heavy component removal tower preferably adopts a packed tower, the pressure at the top of the tower is 9-13 KPa, the pressure at the bottom of the tower is 15-25 KPa, the temperature at the top of the tower is 110-130 ℃, and the temperature at the bottom of the tower is 220-250 ℃.
Separating normal paraffin and isoparaffin in the feed by using an adsorbent in the adsorption tower, and desorbing the normal paraffin by using a desorbent after the normal paraffin is adsorbed by the adsorbent to obtain extract liquid consisting of the normal paraffin and raffinate consisting of the isoparaffin and the desorbent;
the adsorption tower mainly comprises an adsorption chamber, a rotary valve and an adsorption chamber circulating pump which are provided with molecular sieves, and as an optimal technical scheme, the number of the adsorption towers is two, feed liquid between the two adsorption towers circulates through the circulating pump, the feed liquid is pumped out from the bottom of the first adsorption tower by the circulating pump, and the feed liquid enters the top of the second adsorption tower after being pressurized.
Wherein the molecular sieve is 5A molecular sieve. The desorption agent consists of 60 wt% of n-pentane and 40 wt% of isooctane, wherein the n-pentane has the function of desorbing the n-alkane from the cavities of the molecular sieve, and the isooctane has the function of cleaning.
The operating conditions of the adsorption column were: the feeding temperature of the molecular sieve material is 176-180 ℃, the feeding temperature of the desorption agent is 176-180 ℃, and the bottom pressure of the adsorption chamber is 2.2-2.5 MPa.
The raffinate enters a raffinate tower feeding mixing tank and then enters a raffinate tower, the desorbent is distilled out from the top of the tower, the bottom product is isoparaffin fraction, and the operating conditions of the raffinate tower are as follows: the pressure at the top of the tower is 0.15-0.20 Mpa, the pressure at the bottom of the tower is 0.20-0.25 Mpa, the temperature at the top of the tower is 90-100 ℃, the temperature at the bottom of the tower is 240-260 ℃, and the temperature at the lateral line extraction is 115-125 ℃.
Feeding the bottom isoparaffin fraction of the raffinate to a first isoparaffin separation column, wherein the first isoparaffin fraction is distilled from the top of the column, and the operating conditions of the first isoparaffin separation column are as follows: the pressure at the top of the tower is 0.08-0.11Mpa, the pressure at the bottom of the tower is 0.12-0.15Mpa, the temperature at the top of the tower is 198-210 ℃, and the temperature at the bottom of the tower is 270-290 ℃. Taking the tower top fraction of the first isoparaffin separation tower, condensing and cooling the tower top fraction sequentially by a medium-temperature hot oil-isoparaffin separation tower heat exchanger and a low-temperature hot oil-isoparaffin separation tower heat exchanger, and then entering the isoparaffin separation tower reflux tank. The return pump of the isoparaffin separation tower pumps out IP40 isoparaffin from the return tank, the outlet is divided into two paths, one path of isoparaffin is pumped back to the top of the tower to be used as top return, and the other path of isoparaffin passes through the control and regulation valve of the liquid level and the flow cascade of the tank, is cooled by the low-temperature hot oil-IP 40 isoparaffin heat exchanger and the IP40 isoparaffin cooler and then is used as a product IP40 isoparaffin to be stored in the tank area.
By way of comparison, using the process of example 1, with varying ratios of normal to isoparaffins in the feed, it was found that the highest isoparaffins purity was produced when the normal to isoparaffin ratio was in the range of 0.8 to 1.1: 1.
When the ratio of n-alkane to isoparaffin is 2: 1, 2.2: 1, 0.6: 1, 0.7: 1 or 1.3: 1, the separation efficiency of n-alkane and isoparaffin is poor, the life of the molecular sieve is short, and the purity of isoparaffin in the product is only about 90%. More specifically, the ratio of n-alkane to isoparaffin in the raw material is controlled to be 8: 1 for C5-C9 n-alkane, 8: 1 for C5-C9 isoparaffin, 2: 1 for C10-C13 n-alkane, 2: 1 for C10-C13 isoparaffin, 2.2: 1 for C14-C16 n-alkane, C14-C16 isoparaffin, and 2.1: 1 for C17+ n-alkane, C17+ isoparaffin. The separation efficiency of normal paraffin and isoparaffin is poor, the service life of the molecular sieve is short, and the purity of isoparaffin in the product is only 90%.
By way of comparison, using the process of example 1, when the feed contained 2 wt% naphthenes, the isoparaffins produced were of low purity, only 88%.
Claims (9)
1. The isoparaffin solvent oil composition prepared by taking coal indirect liquefied product as raw material is characterized in that the raw material is subjected to 5A molecular sieve adsorption, rectification and cutting processes to obtain isoparaffin, the raw material source is that a first coal indirect liquefied Fischer-Tropsch product and a second coal indirect liquefied Fischer-Tropsch product are blended according to a certain volume ratio, the weight ratio of normal paraffin to isoparaffin is (0.8-1.1) to 1, and the flash point of the prepared isoparaffin solvent oil composition is 45-61 ℃.
2. The isoparaffin solvent oil composition of claim 1, wherein the normal paraffins content of the coal indirect liquefaction first fischer-tropsch product is greater than 90%, wherein the normal paraffins from C9-C18 account for more than 96% of the total normal paraffins, and the isoparaffin content of the coal indirect liquefaction second fischer-tropsch product is greater than 85%, wherein the isoparaffins from C9-C20 account for more than 96% of the total isoparaffins.
3. The isoparaffinic solvent oil composition according to claim 1 or 2, wherein the purity of the isoparaffinic solvent oil composition is greater than 96%.
4. The isoparaffinic solvent oil composition according to claim 3, wherein the purity of the isoparaffinic solvent oil composition is greater than 97%.
5. The isoparaffin solvent oil composition according to any one of claims 1 to 4, wherein the distillation cut process comprises the isoparaffin separation column at an overhead pressure of 0.08 to 0.11MPa, a bottom pressure of 0.12 to 0.15MPa, an overhead temperature of 198- > 210 ℃ and a bottom temperature of 270- > 290 ℃.
6. The isoparaffinic solvent oil composition according to any one of claims 1 to 5, wherein the isoparaffinic solvent oil composition is 2-methylnonane: 47.9%, isomeric C11: 50.5%, isomeric C12: 0.5%, normal C9-C11: 0.1%, and the distillation range is 170-.
7. The isoparaffinic solvent oil composition according to any one of claims 1 to 6, wherein said isoparaffin contains no naphthenes and has an aromatic content of less than 50 ppm.
8. The isoparaffin solvent oil composition according to any one of claims 1 to 7, wherein in the feed, the ratio of C5-C9 normal paraffins to C5-C9 isoparaffins to (2-5) to 1, the ratio of C10-C13 normal paraffins to C10-C13 isoparaffins to (0.8-1) to 1, the ratio of C14-C16 normal paraffins to C14-C16 isoparaffins to (1-1.2) to 1, and the ratio of C17+ normal paraffins to C17+ isoparaffins to (1-1.2) to 1.
9. The isoparaffinic solvent oil composition according to any one of claims 1 to 7, wherein neither the coal-mediated liquefied first Fischer-Tropsch product nor the second Fischer-Tropsch product contains naphthenes, nitrogen, and sulfur.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113667527A (en) * | 2021-08-20 | 2021-11-19 | 卓链化工(上海)有限公司 | Preparation method of plastic release agent containing isoparaffin |
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| CN109161399A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of liquid hydrocarbon composition containing isoparaffin component |
| CN109161397A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of isoparaffin solvent oil composition |
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- 2019-01-23 CN CN201910060902.7A patent/CN111471486A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20040004021A1 (en) * | 2000-07-26 | 2004-01-08 | Eric Benazzi | Flexible method for producing oil bases and distillates from feedstock containing heteroatoms |
| CN107312569A (en) * | 2016-04-26 | 2017-11-03 | 神华集团有限责任公司 | A kind of method of F- T synthesis naphtha production isoparaffin solvent oil and the isoparaffin solvent oil obtained by this method |
| CN109161399A (en) * | 2018-10-11 | 2019-01-08 | 内蒙古伊泰宁能精细化工有限公司 | A kind of liquid hydrocarbon composition containing isoparaffin component |
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| CN113667527A (en) * | 2021-08-20 | 2021-11-19 | 卓链化工(上海)有限公司 | Preparation method of plastic release agent containing isoparaffin |
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