CN1919809A - Energy-saving technique for producing high-purity pentane and pentane foaming agent - Google Patents
Energy-saving technique for producing high-purity pentane and pentane foaming agent Download PDFInfo
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- CN1919809A CN1919809A CN 200610014353 CN200610014353A CN1919809A CN 1919809 A CN1919809 A CN 1919809A CN 200610014353 CN200610014353 CN 200610014353 CN 200610014353 A CN200610014353 A CN 200610014353A CN 1919809 A CN1919809 A CN 1919809A
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Abstract
The invention discloses a saving technology of high-purity pantane and pantane foaming agent, which is characterized by the following: adopting topped crude or any one of other source materials or random proportional compounds as raw material; heating; pressurizing; connecting dehydrogenizing tower 2, isopentane tower 3, composite pantane tower 4, n-pentane tower 5 and cyclopentene 6 sequently; distilling; obtaining composite pantane as pantane foaming agent.
Description
Technical field
The present invention relates to utilize the carbon five of by-product cracking c_5, refinery, oil field and Sweet natural gas recovery in the petroleum hydrocarbon cracking ethylene preparation device, tops and the carbon five resources production high-purity pentane in other source and the technology of pentane foaming agent of reformer.
Background technology
The growth of pentane consumption and freonll-11 forbidding have direct relation, the Montreal protocol that passes through according to various countries in 1992, require various countries to stop using ozonosphere depleting substance freonll-11 in 2000, pentane is as final substitute products, and the coming years, its development potentiality was huge.Pentane foaming agent is the different ratios mixture of iso-pentane, Skellysolve A and pentamethylene single component and iso-pentane, Skellysolve A or iso-pentane, pentamethylene.The comprehensive utilization that is mainly derived from carbon five resources of present domestic pentane.
Carbon five resources comprise carbon five, the tops of reformer and the carbon five in other source that by-product cracking c_5, refinery, oil field and the Sweet natural gas in the petroleum hydrocarbon cracking ethylene preparation device reclaims, and wherein cracking c_5 is the main source of carbon five resources.World today's ethylene industry is still developing rapidly, and the throughput of petroleum hydrocarbon cracking ethylene preparation device constantly increases, and to adopt liquid hydrocarbon be that the device of cracking stock increases gradually, and indicating can be abundant day by day for the cracking c_5 resource of utilizing.The isolation technique of C5 fraction comprises and adopts extraction technique to produce unsaturated hydrocarbons products such as isoprene and cyclopentenes, but the raffinate carbon-5 that contains a large amount of stable hydrocarbon can only fail to make full use of at present as gasoline blend component or domestic fuel.
The production method of present pentane foaming agent is: at first the carbon Wuyuan is expected that rectifying separation becomes iso-pentane, Skellysolve A and pentamethylene successively, and then reconcile into the pentane foaming agent product according to customer requirements that the ratio of each component is as follows in the common pentane foaming agent product:
Skellysolve A: iso-pentane is 8: 2
Skellysolve A: iso-pentane is 7: 3
Skellysolve A: iso-pentane is 6: 4
Skellysolve A: iso-pentane is 5: 5
Pentamethylene: iso-pentane is 67: 32
Use at present maximum pentane foaming agent products be just only containing, the hybrid pentane and the pentamethylene single component of iso-pentane.
Conventional production method is that the iso-pentane in the raw material, Skellysolve A and pentamethylene are separated each other fully, and then reconciles into product, and this " separates remix earlier ", and process is actually a kind of loss of energy, and unreasonable.
Summary of the invention
The objective of the invention is to overcome the prior art production energy consumption high deficiency, it is raw material that a kind of carbon five, the tops of reformer or carbon five in other source that reclaims with the by-product cracking c_5 in the ethylene unit behind the hydrogenation, refinery, oil field and Sweet natural gas is provided, and adopts technical combinations such as precise distillation and light constituent enrichment to produce the energy-saving technique of high-purity pentane and pentane foaming agent.
The object of the present invention is achieved like this:
A kind of energy-saving technique of producing high-purity pentane and pentane foaming agent, cracking c_5 or etherificate carbon five behind the employing hydrogenation, refinery, the carbon five that oil field and Sweet natural gas reclaim, any carbon Wuyuan material in the tops of reformer or other source or the mixture of their arbitrary proportions are raw material, after raw material pressurizes through heating from head tank, via lightness-removing column 2, iso-pentane tower 3, hybrid pentane tower 4, Skellysolve A tower 5, the pentamethylene tower 6 five-stages compression rectification tower of heating is linked in sequence, continuous rectification obtains iso-pentane from the iso-pentane tower respectively, obtain Skellysolve A from the Skellysolve A tower, from the pentamethylene tower obtain pentamethylene and from the hybrid pentane tower obtain can be directly as the hybrid pentane of pentane foaming agent.
Described each stage process condition is as follows: the head tank feeding temperature is a normal temperature, pressure is 0.55～1.0MPa, after being preheated to 80～100 ℃, preheater 1 enters lightness-removing column 2 middle parts, from removed overhead carbon 4 components, lightness-removing column 2 is a pressurized operation, is structured packing and sparger in the tower, working pressure is 0.55～0.85MPa, tower top temperature is 55～77 ℃, and column bottom temperature is 97～118 ℃, and production S3 enters iso-pentane tower 3 at the bottom of the tower; The iso-pentane tower is a pressurized operation, be structured packing and sparger in the tower, working pressure is 0.25～0.45MPa, tower top temperature is 57～79 ℃, column bottom temperature is 73～94 ℃, and the iso-pentane column overhead is provided with light constituent enrichment section, and the light constituent S4 of cat head enrichment returns head tank, iso-pentane product S5 is by the side line extraction, and production S6 enters hybrid pentane tower 4 at the bottom of the tower; The hybrid pentane tower is a pressurized operation, is structured packing and sparger in the tower, and working pressure is 0.25～0.45MPa, and tower top temperature is 64～80 ℃, and column bottom temperature is 77～95 ℃, and hybrid pentane S7 is by this column overhead extraction, and production S8 enters Skellysolve A tower 5 at the bottom of the tower; The Skellysolve A tower is a pressurized operation, be structured packing and sparger in the tower, working pressure is 0.25～0.45MPa, tower top temperature is 64～88 ℃, column bottom temperature is 82～105 ℃, and this column overhead is provided with light constituent enrichment section, and the light constituent S9 of cat head enrichment returns head tank, highly purified Skellysolve A product S10 is by the side line extraction, and production S11 enters pentamethylene tower 6 at the bottom of the tower; The pentamethylene tower is a pressurized operation, be structured packing and sparger in the tower, working pressure is 0.15～0.45MPa, tower top temperature is 61.3～103 ℃, column bottom temperature is 91～112 ℃, and this column overhead is provided with light constituent enrichment section, and the light constituent S12 of cat head enrichment returns head tank, highly purified cyclopentane product S13 is by the side line extraction, extraction heavy constituent S14 at the bottom of the tower;
Obviously, in actual applications, production unit can be by changing the hybrid pentane tower cat head and the content of adjusting iso-pentane in the hybrid pentane product arbitrarily of the produced quantity at the bottom of the tower, make its product standard that reaches pentane foaming agent, other pentane foaming agent product can by iso-pentane, hybrid pentane, Skellysolve A and pentamethylene arbitrarily both mixing produce.
Advantage of the present invention is:
1, product purity height, the purity of the various pentane products of being produced can reach more than 99.8% (quality).
But 2 direct production only contain the pentane foaming agent product export of iso-pentane and two kinds of component arbitrary proportions of Skellysolve A, need not to be in harmonious proportion.
3, since iso-pentane do not need to separate fully with Skellysolve A so than existing energy saving technology.
4, because the various pentane product purity height that this technology is produced, and can direct production go out the hybrid pentane that only contains iso-pentane and two kinds of component arbitrary proportions of Skellysolve A as the pentane foaming agent product, and do not need various pentanes are separated fully, so cost reduces significantly.
Description of drawings
Fig. 1 is a process flow sheet of the present invention; Wherein, 1-preheater; The 2-lightness-removing column; 3-iso-pentane tower; 4-hybrid pentane tower; 5-Skellysolve A tower; 6-changes pentanizer; The S1-raw material; The S2-C4 component; S4, S9, S12-light constituent; S3, S6, S8, S11-tower bottoms; The S5-iso-pentane; The S7-hybrid pentane; The S10-Skellysolve A; The S13-pentamethylene; The S14-heavy constituent.
Embodiment
Below in conjunction with accompanying drawing the present invention is described in further detail the present invention:
Referring to accompanying drawing 1, a kind of energy-saving technique of producing high-purity pentane and hybrid pentane, cracking c_5 or etherificate carbon five behind the employing hydrogenation, refinery, the carbon five that oil field and Sweet natural gas reclaim, any carbon Wuyuan material in the tops of reformer or other source or the mixture of their arbitrary proportions are raw material S1, after raw material pressurizes through heating from head tank, via lightness-removing column 2, iso-pentane tower 3, hybrid pentane tower 4, Skellysolve A tower 5, the pentamethylene tower 6 five-stages compression rectification tower of heating is linked in sequence, continuous rectification obtains iso-pentane S5 from the iso-pentane tower respectively, obtain Skellysolve A S10 from the Skellysolve A tower, obtain pentamethylene S13 and obtain hybrid pentane S7 from the pentamethylene tower from the hybrid pentane tower.
Embodiment 1:
With cracking c_5 behind the hydrogenation is raw material, and the raw material composition sees the following form:
| Component | Content (quality) |
| Propane iso-butane normal butane isopentane pentane 2; 2-dimethylbutane pentamethylene 2-methylpentane 3-methylpentane n-hexane 2,2-dimethyl pentane benzene: | 0.01％ 0.04％ 1.56％ 33.57％ 32.85％ 0.23％ 27.68％ 3.25％ 0.56％ 0.08％ 0.02％ 0.15％ |
The temperature of charging S1 is a normal temperature, be forced into 0.55MPa, after being preheated to 80.0 ℃, preheater 1 enters lightness-removing column 2 middle parts, from removed overhead C4 component S 2, in the lightness-removing column is structured packing of Lamb wave type and secondary grooved sparger, and working pressure is 0.55MPa, and tower top temperature is 55 ℃, column bottom temperature is 97 ℃, and production S3 enters iso-pentane tower 3 at the bottom of the tower; In the iso-pentane Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.25MPa, tower top temperature is 57 ℃, column bottom temperature is 73 ℃, this column overhead is provided with light constituent enrichment section, and the light constituent S4 of cat head enrichment returns head tank, purity 〉=99.0% (w/w, iso-pentane product S5 down together) is by the side line extraction, and production S6 enters hybrid pentane tower 4 at the bottom of the tower; In the hybrid pentane Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.25MPa, and tower top temperature is 57.6 ℃, and column bottom temperature is 77 ℃, contain iso-pentane 90% and Skellysolve A 10% hybrid pentane S7 by this column overhead extraction, production S8 enters Skellysolve A tower 5 at the bottom of the tower; In the Skellysolve A Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.25MPa, tower top temperature is 64 ℃, column bottom temperature is 82 ℃, this column overhead is provided with light constituent enrichment section, the light constituent S9 of cat head enrichment returns head tank, and purity 〉=99.0% Skellysolve A S10 product is by the side line extraction, and production S11 enters the pentamethylene tower at the bottom of the tower; In the pentamethylene Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.25MPa, tower top temperature is 79 ℃, column bottom temperature is 91 ℃, this column overhead is provided with light constituent enrichment section, the light constituent S12 of cat head enrichment returns head tank, and the cyclopentane product S13 of purity 〉=99.0% is by the side line extraction, extraction heavy constituent S14 at the bottom of the tower.
Embodiment 2:
Raw material is with example 1, the temperature of charging S1 is a normal temperature, be forced into 1.0MPa, entering lightness-removing column 2 middle parts after preheater 1 is preheated to 100 ℃, from removed overhead C4 component S 2, is structured packing of Lamb wave type and secondary grooved sparger in the lightness-removing column, working pressure is 0.85MPa, tower top temperature is 77 ℃, and column bottom temperature is 118 ℃, and production S3 enters iso-pentane tower 3 at the bottom of the tower; In the iso-pentane Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.45MPa, tower top temperature is 79 ℃, column bottom temperature is 94 ℃, this column overhead is provided with light constituent enrichment section, and the light constituent S4 of cat head enrichment returns head tank, purity 〉=99.0% (w/w, iso-pentane product S5 down together) is by the side line extraction, and production S6 enters hybrid pentane tower 4 at the bottom of the tower; In the hybrid pentane Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.45MPa, and tower top temperature is 86.8 ℃, and column bottom temperature is 95 ℃, contain iso-pentane 10% and Skellysolve A 90% hybrid pentane S7 by this column overhead extraction, production S8 enters Skellysolve A tower 5 at the bottom of the tower; In the Skellysolve A Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.45MPa, tower top temperature is 88 ℃, column bottom temperature is 105 ℃, this column overhead is provided with light constituent enrichment section, the light constituent S9 of cat head enrichment returns head tank, and purity 〉=99.0% Skellysolve A S10 product is by the side line extraction, and production S11 enters the pentamethylene tower at the bottom of the tower; In the pentamethylene Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.45MPa, tower top temperature is 103 ℃, column bottom temperature is 112 ℃, this column overhead is provided with light constituent enrichment section, the light constituent S12 of cat head enrichment returns head tank, and the cyclopentane product S13 of purity 〉=99.0% is by the side line extraction, extraction heavy constituent S14 at the bottom of the tower.
Embodiment 3:
With unreacted carbon five in the tert amyl methyl ether(TAME) method behind the hydrogenation is raw material, and the raw material composition sees the following form:
| Component | Content (quality) |
| Normal butane isopentane pentane pentamethylene 2-methylpentane 3-methylpentane n-hexane methyl cyclopentane benzene: | 2.2％ 23.3％ 52.9％ 11.2％ 4.9％ 1.1％ 2.4％ 0.4％ 1.6％ |
The temperature of raw material S1 is a normal temperature, be forced into 0.55MPa and after preheater 1 is preheated to 98.0 ℃, enter lightness-removing column 2 middle parts, from removed overhead C4 component S 2, in the lightness-removing column is structured packing of Lamb wave type and secondary grooved sparger, working pressure is 0.6MPa, tower top temperature is 61.3 ℃, and column bottom temperature is 104.4 ℃, and production S3 enters iso-pentane tower 3 at the bottom of the tower; In the iso-pentane Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.25MPa, tower top temperature is 56.2 ℃, column bottom temperature is 73.8 ℃, this column overhead is provided with light constituent enrichment section, and the light constituent S4 of cat head enrichment returns head tank, purity 〉=99.8% (w/w, iso-pentane S5 product down together) is by the side line extraction, and production S6 enters hybrid pentane tower 4 at the bottom of the tower; In the hybrid pentane Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.25MPa, tower top temperature is 62.5 ℃, column bottom temperature is 77.1 ℃, the hybrid pentane product S7 that contains iso-pentane 30% and Skellysolve A 70% is by this column overhead extraction, and production S8 enters Skellysolve A tower 5 at the bottom of the tower; In the Skellysolve A Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.25MPa, tower top temperature is 64.5 ℃, column bottom temperature is 92.0 ℃, this column overhead is provided with light constituent enrichment section, the light constituent S9 of cat head enrichment returns head tank, and purity 〉=99.8% Skellysolve A product S10 is by the side line extraction, and production S11 enters pentamethylene tower 6 at the bottom of the tower; In the pentamethylene Tata is structured packing of silk screen type and secondary grooved sparger, working pressure is 0.15MPa, tower top temperature is 61.3 ℃, column bottom temperature is 86.7 ℃, this column overhead is provided with light constituent enrichment section, the light constituent S12 of cat head enrichment returns head tank, and the cyclopentane product S13 of purity 〉=99.8% is by the side line extraction, extraction heavy constituent S14 at the bottom of the tower.
The invention discloses the energy-saving technique that utilizes carbon five resources to produce high-purity pentane and pentane foaming agent, those skilled in the art can be by using for reference this paper content, and links such as appropriate change processing parameter, structure design realize.System of the present invention is described by preferred embodiments, and person skilled obviously can be changed or suitably change and combination system as herein described in not breaking away from content of the present invention, spirit and scope, realizes the technology of the present invention.Special needs to be pointed out is that replacement that all are similar and change all are conspicuous for a person skilled in the art, they all are regarded as being included in spirit of the present invention, scope and the content.
Claims (10)
1, a kind of energy-saving technique of producing high-purity pentane and hybrid pentane, cracking c_5 or etherificate carbon five behind the employing hydrogenation, refinery, the carbon five that oil field and Sweet natural gas reclaim, any carbon Wuyuan material in the tops of reformer or other source or the mixture of their arbitrary proportions are raw material, after raw material pressurizes through heating from head tank, by lightness-removing column [2], iso-pentane tower [3], hybrid pentane tower [4], Skellysolve A tower [5], pentamethylene tower [6] the five-stage compression rectification tower of heating is linked in sequence, and obtains iso-pentane from the iso-pentane tower respectively through continuous rectification, obtain Skellysolve A from the Skellysolve A tower, obtain pentamethylene and obtain hybrid pentane from the pentamethylene tower from the hybrid pentane tower.
2, the energy-saving technique of production high-purity pentane according to claim 1 and hybrid pentane, it is characterized in that: the head tank feeding temperature is a normal temperature, is forced into 0.55～1.0MPa, enters lightness-removing column [2] middle part after preheater [1] is preheated to 80～100 ℃.
3, the energy-saving technique of production high-purity pentane according to claim 1 and hybrid pentane, it is characterized in that: lightness-removing column [2] is a pressurized operation, be structured packing and sparger in the tower, from removed overhead carbon 4 components, working pressure is 0.55～0.85MPa, tower top temperature is 55～77 ℃, and column bottom temperature is 97～118 ℃, and production S3 enters iso-pentane tower [3] at the bottom of the tower.
4, the energy-saving technique of production high-purity pentane according to claim 1 and hybrid pentane, it is characterized in that: iso-pentane tower [3] is a pressurized operation, be structured packing and sparger in the tower, working pressure is 0.25～0.45MPa, tower top temperature is 57～79 ℃, column bottom temperature is 73～94 ℃, and iso-pentane product S5 is by the side line extraction, and production S6 enters hybrid pentane tower [4] at the bottom of the tower.
5, the energy-saving technique of production high-purity pentane according to claim 4 and hybrid pentane is characterized in that: the iso-pentane column overhead is provided with light constituent enrichment section, and the light constituent S4 of cat head enrichment returns head tank.
6, the energy-saving technique of production high-purity pentane according to claim 1 and hybrid pentane, it is characterized in that: hybrid pentane tower [4] is a pressurized operation, be structured packing and sparger in the tower, working pressure is 0.25～0.45MPa, tower top temperature is 57.6～86.8 ℃, column bottom temperature is 77～95 ℃, and hybrid pentane S7 is by the cat head extraction, and production S8 enters Skellysolve A tower [5] at the bottom of the tower.
7, the energy-saving technique of production high-purity pentane according to claim 1 and hybrid pentane, it is characterized in that: Skellysolve A tower [5] is a pressurized operation, be structured packing and sparger in the tower, working pressure is 0.25～0.45MPa, tower top temperature is 64～88 ℃, column bottom temperature is 82～105 ℃, and highly purified Skellysolve A product S10 is by the side line extraction, and production S11 enters pentamethylene tower [6] at the bottom of the tower.
8, according to the energy-saving technique of claim 1 or 7 described production high-purity pentanes and hybrid pentane, it is characterized in that: Skellysolve A tower [5] cat head is provided with light constituent enrichment section, and the light constituent S9 of cat head enrichment returns head tank.
9, the energy-saving technique of production high-purity pentane according to claim 1 and hybrid pentane, it is characterized in that: pentamethylene tower [6] is a pressurized operation, be structured packing and sparger in the tower, working pressure is 0.15～0.45MPa, tower top temperature is 61.3～103 ℃, column bottom temperature is 91～112 ℃, and highly purified cyclopentane product S13 is by the side line extraction, extraction heavy constituent S14 at the bottom of the tower.
10, according to the energy-saving technique of claim 1 or 9 described production high-purity pentanes and hybrid pentane, it is characterized in that: pentamethylene Tata [6] top is provided with light constituent enrichment section, and the light constituent S12 of cat head enrichment returns head tank.
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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101823931A (en) * | 2010-05-13 | 2010-09-08 | 天津大学 | Method for deeply processing C5 raffinate raw material separated from diolefin |
| CN103073376A (en) * | 2013-02-22 | 2013-05-01 | 南京炼油厂有限责任公司 | Separation process of mixed pentane |
| CN104710262A (en) * | 2015-02-12 | 2015-06-17 | 新疆独山子天利实业总公司 | Method for producing pentane foaming agent with a difference ratio of isopentane to n-pentane being 5:5 |
| CN104725180A (en) * | 2015-02-12 | 2015-06-24 | 新疆独山子天利实业总公司 | Method for producing pentane foaming agent with different direct ratio of 3:7 |
| CN105949026A (en) * | 2016-06-27 | 2016-09-21 | 河南中托力合化学有限公司 | Mixed pentane precise separation device |
| 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 |
| CN107739290A (en) * | 2017-09-16 | 2018-02-27 | 濮阳市联众兴业化工有限公司 | A kind of method that cracking c_5 prepares pentane foaming agent |
| CN107759435A (en) * | 2017-09-16 | 2018-03-06 | 濮阳市联众兴业化工有限公司 | A kind of method for removing pentamethylene stink |
| CN107778128A (en) * | 2016-08-25 | 2018-03-09 | 邢台旭阳科技有限公司 | A kind of method that high-purity pentamethylene is extracted in two steps rectifying from non-aromatic hydrocarbon ils |
| CN109305877A (en) * | 2017-07-26 | 2019-02-05 | 抚顺伊科思新材料有限公司 | Thick light dydrocarbon produces high alkene light dydrocarbon, pentane, isopentane and pentamethylene method |
| CN111362773A (en) * | 2020-04-24 | 2020-07-03 | 河北新启元能源技术开发股份有限公司 | Equipment and process for preparing pentane foaming agent by reforming topped naphtha |
| CN112374958A (en) * | 2020-11-12 | 2021-02-19 | 北方华锦化学工业股份有限公司 | Method for producing isopentane by hydrocracking naphtha |
| CN112778073A (en) * | 2021-01-05 | 2021-05-11 | 中国神华煤制油化工有限公司 | Method for preparing pentane from coal-based mixed pentene and application thereof |
| 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 |
| CN115974639A (en) * | 2023-03-21 | 2023-04-18 | 新疆天利石化股份有限公司 | Method for co-production of methylcyclopentane by cracking carbon nine hydrogenation device and pentane device |
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| CN101823931A (en) * | 2010-05-13 | 2010-09-08 | 天津大学 | Method for deeply processing C5 raffinate raw material separated from diolefin |
| CN101823931B (en) * | 2010-05-13 | 2013-06-26 | 天津大学 | Method for deeply processing C5 raffinate raw material separated from diolefin |
| CN103073376A (en) * | 2013-02-22 | 2013-05-01 | 南京炼油厂有限责任公司 | Separation process of mixed pentane |
| CN104710262A (en) * | 2015-02-12 | 2015-06-17 | 新疆独山子天利实业总公司 | Method for producing pentane foaming agent with a difference ratio of isopentane to n-pentane being 5:5 |
| CN104725180A (en) * | 2015-02-12 | 2015-06-24 | 新疆独山子天利实业总公司 | Method for producing pentane foaming agent with different direct ratio of 3:7 |
| CN105949026A (en) * | 2016-06-27 | 2016-09-21 | 河南中托力合化学有限公司 | Mixed pentane precise separation device |
| CN107778128A (en) * | 2016-08-25 | 2018-03-09 | 邢台旭阳科技有限公司 | A kind of method that high-purity pentamethylene is extracted in two steps rectifying from non-aromatic hydrocarbon ils |
| CN109305877A (en) * | 2017-07-26 | 2019-02-05 | 抚顺伊科思新材料有限公司 | Thick light dydrocarbon produces high alkene light dydrocarbon, pentane, isopentane and pentamethylene method |
| CN107759435A (en) * | 2017-09-16 | 2018-03-06 | 濮阳市联众兴业化工有限公司 | A kind of method for removing pentamethylene stink |
| CN107739290A (en) * | 2017-09-16 | 2018-02-27 | 濮阳市联众兴业化工有限公司 | A kind of method that cracking c_5 prepares pentane foaming agent |
| CN107759435B (en) * | 2017-09-16 | 2020-08-11 | 濮阳市联众兴业化工有限公司 | Method for removing odor of cyclopentane |
| 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 |
| CN111362773A (en) * | 2020-04-24 | 2020-07-03 | 河北新启元能源技术开发股份有限公司 | Equipment and process for preparing pentane foaming agent by reforming topped naphtha |
| CN112374958A (en) * | 2020-11-12 | 2021-02-19 | 北方华锦化学工业股份有限公司 | Method for producing isopentane by hydrocracking naphtha |
| CN112778073A (en) * | 2021-01-05 | 2021-05-11 | 中国神华煤制油化工有限公司 | Method for preparing pentane from coal-based mixed pentene and application thereof |
| 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 |
| CN115974639A (en) * | 2023-03-21 | 2023-04-18 | 新疆天利石化股份有限公司 | Method for co-production of methylcyclopentane by cracking carbon nine hydrogenation device and pentane device |
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