CN114276834B - Preparation method of refined C5 fraction - Google Patents
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Abstract
The invention relates to a preparation method of refined C5 fraction, which comprises the following steps: adding crude C5 olefins into a high-pressure reaction kettle with a stirrer in advance, adding a catalyst under the protection of nitrogen for isomerization reaction, removing impurities by adopting the processes of extractive distillation, fine filtration and the like of a composite solvent, and selectively hydrogenating and saturating residual alkyne and part of diene to obtain C5 olefin fraction enriched with beta-monoolefine, wherein the C5 olefin fraction can be applied to the fields of resin synthesis, modification and the like.
Description
Technical Field
The invention belongs to the field of organic chemical industry, and particularly relates to a preparation method of refined C5 fraction.
Background
A large amount of cracked C5 fractions are produced in the process of preparing ethylene by naphtha cracking, and diolefins such as Isoprene (IP), dicyclopentadiene (DCPD), piperylene (PD) and the like can be obtained by the processes of extractive distillation separation or thermal dimerization distillation and the like, so that the method is used for downstream production of numerous chemical products with higher economic added values. The refined C5 generated in the process of cracking C5 to separate diolefin and the unpolymerized C5 generated in the process of resin polymerization are collectively called raffinate C5, and the refined C5 and the unpolymerized C5 are mainly used as light raw materials of oil products to reduce the cost at present and have low additional value.
The C5 after etherification generally refers to light hydrocarbons mainly comprising mono-olefins such as 1-pentene, 2-pentene, isoamylene, cyclopentene and the like, which are derived from a byproduct of an isoamylene extraction unit and a byproduct of an MTO unit. According to different processes, the catalyst also contains butyne, isopenteneyne, isopropyl acetylene and other components. For example, in an MTO device, products of ethylene and propylene are extracted and rectified by dimethyl ether to obtain C4-C6 fractions containing a large amount of unsaturated olefins, which are generally called C4 after-ether. After C4 components such as isobutene, butadiene and the like are separated and recovered, the residual fraction can only be used as a raw material for preparing pentane and hexane by hydrogenation generally because a large amount of alkyne is still contained.
In view of the above-mentioned low value-added C5 olefins in petrochemical industry, research in industry has generally focused on processes for obtaining saturated paraffins by hydrogenation reactions. In patent CN1348941a, gasoline blending component TAME without lead, containing oxygen and having high octane number is obtained by cracking C5 fraction through isoprene removal, selective hydrogenation, etherification reaction and saturated hydrogenation technologies.
The influence of the nitride of the light oil product is far greater than that of other impurities, particularly, the nitride generates colloid precipitate in the storage process and reacts with alkyne to form photosensitive components, so that the quality of the oil product is deteriorated. Researchers at home and abroad such as Shang Yazhuo study on the treatment of light oil products by different processes such as hydrofining, clay refining, acid-base combined refining and the like, remove partial inorganic and organic impurities containing nitrogen and sulfur, and improve the quality of the oil products.
However, in the above process, the treatment of impurities in C5 olefins or light raw materials and the selective hydrogenation to obtain high octane number and low impurity oil products are mainly considered, and the targeted optimization of components in C5 fraction by the composite process has not been reported or studied.
Disclosure of Invention
Aiming at the defects of the prior art, the technical problem to be solved by the invention is to provide a preparation method for refining a C5 fraction.
The invention relates to a preparation method of a beta-monoolefin enriched C5 olefin fraction, which comprises the following steps:
(1) Under the protection of nitrogen, adding a catalyst into crude C5 olefin, carrying out isomerization reaction for 1-30 min at-5-25 ℃, adjusting the pH value of the C5 olefin to 6-8 by activated clay, then extracting and rectifying under the action of a composite solvent, and then entering an adsorption packed bed to obtain C5 fraction A;
(2) The C5 fraction A is subjected to Pd/Al modification 2 O 3 With H under the action of a catalyst 2 Selectively hydrogenating at 25-65 deg.c and 0.8-1.5 MPa and liquid hourly space velocity LHSV of 1-20 hr -1 And the hydrogen-oil ratio is (1-200) to 1, so as to obtain the beta-olefin-enriched C5 fraction B.
The preferred mode of the above preparation method is as follows:
the step (1) is specifically as follows: adding crude C5 olefin into a high-pressure reaction kettle with a stirrer in advance, adding 0.01-0.5 wt% of super-strong base catalyst under the protection of nitrogen, carrying out isomerization reaction for 1-30 min at-5-25 ℃, filtering alkaline mechanical impurities by activated clay, adjusting the pH value to 6-8, conveying to an extraction rectifying tower, removing alkyne by extraction and rectification under the action of a composite solvent, and then entering an adsorption packed bed to remove trace water, impurities and the like to obtain C5 fraction A.
The crude C5 olefin in the step (1) comprises the following components: 0 to 0.30 percent of 1-butyne, 0.01 to 0.5 percent of trans-2-butene, 0.01 to 0.8 percent of cis-2-pentene, 0.1 to 2.0 percent of 3-methyl-1-butene, 5.0 to 40.0 percent of isopentane, 0.01 to 2.0 percent of 1,4-pentadiene, 0.01 to 0.2 percent of 2-butyne, 0.5 to 10.0 percent of 1-pentene, 0.01 to 5.0 percent of isopentene, 0.5 to 20.0 percent of 2-methyl-1-butene, 0.5 to 40.0 percent of n-pentane, 0.1 to 5.0 percent of isoprene, 1.0 to 20 percent of trans-2-pentene, 1.0 to 15 percent of cis-2-pentene, 0.01 to 0.5 percent of 1-pentyne, 1.0 to 25 percent of 2-methyl-2-butene, 0.1.1 to 3.0 percent of trans-5262 zxft 0.1 to 3.63 percent of cyclopentadiene, 0.1 to 10.1 zxft And 0 to 10 percent of the rest of cyclopentane, 0.1 to 3.0 to 10 percent of C.
The catalyst in the step (1) is a super-strong base catalyst; the super alkali catalyst is Na-MgO, na/gamma-Al 2 O 3 、Na-NaOH/γ-Al 2 O 3 、K-KOH/γ-Al 2 O 3 、K-NaOH/γ-Al 2 O 3 、KNO 3 /γ-Al 2 O 3 One or more of the above; the adding amount of the catalyst is 0.01 to 0.5 weight percent of the total material.
The composite solvent in the step (1) is a mixed solution of furfural and DMF; wherein the mass ratio of the furfural to the DMF is (1-5) to 1. The extraction and rectification in the step (1) is specifically as follows: the solvent ratio is 0.4-0.6, the rectification reflux ratio is 2-3, the feeding temperature of the extraction tower is 35-70 ℃, the tower top temperature is 40-75 ℃, the tower kettle temperature is 60-120 ℃, and the operating pressure is 0.12-0.20 MPa.
The packing in the adsorption packed bed in the step (1) is as follows: the upper layer is a 20-60 mu m foam porous titanium plate, and the lower layer is 3-6 mm spherical alumina; the operating temperature of the packed bed is 5-40 ℃, and the operating pressure is 0.1-0.3 MPa.
The composition of fraction a comprises: 0 to 0.10 percent of 1-butyne, 0.01 to 0.5 percent of trans-2-butene, 0.01 to 0.8 percent of cis-2-pentene, 0.1 to 1.5 percent of 3-methyl-1-butene, 5.0 to 40.0 percent of isopentane, 0.01 to 2.0 percent of 1,4-pentadiene, 0.01 to 0.05 percent of 2-butyne, 0.5 to 10.0 percent of 1-pentene, 0.01 to 0.5 percent of isopentene, 0.1 to 10.0 percent of 2-methyl-1-butene, 0.5 to 40.0 percent of n-pentane, 0.1 to 5.0 percent of isoprene, 1.0 to 20 percent of trans-2-pentene, 1.0 to 15 percent of cis-2-pentene, 0.01 to 0.10 percent of 1-pentyne, 1.0 to 35 percent of 2-methyl-2-butene, 0.1.1 to 3.0 percent of trans-5262 zxft 0.1 to 3.63 percent of cyclopentadiene, 0.1 to 0.1 zxft, 0 to 10 percent of the rest of cyclopentane, 0.6 to 0 to 3.1 to 0 percent of C.
The step (2) is specifically as follows: the fraction A is conveyed to a hydrogenation reactor and is subjected to Pd/Al modification 2 O 3 With H under the action of a catalyst 2 Selective hydrogenation is carried out at the temperature of 25-65 ℃ and the pressure of 0.8-1.5 MPa, and the Liquid Hourly Space Velocity (LHSV) is 1-20 h -1 And the hydrogen-oil ratio is (1-200) to 1, and finally the C5 fraction B enriched with beta-olefin is obtained.
The modified Pd/Al in the step (2) 2 O 3 The catalyst has main catalyst Pd content of 0.1-2.0 wt% and modified component Y, ce or Pr content of 0.03-1.0 wt%.
The composition of the fraction B in the step (2) comprises: 0.01 to 0.2 percent of trans-2-butene, 0.01 to 0.2 percent of cis-2-pentene, 0.1 to 1.5 percent of 3-methyl-1-butene, 5.0 to 45.0 percent of isopentane, 0.01 to 0.5 percent of 1,4-pentadiene, 0.5 to 8.0 percent of 1-pentene, 0.1 to 10.0 percent of 2-methyl-1-butene, 0.5 to 43.0 percent of n-pentane, 0.1 to 3.0 percent of isoprene, 0.5 to 15 percent of trans-2-pentene, 0.5 to 10 percent of cis-2-pentene, 1.0 to 33 percent of 2-methyl-2-butene, 0.1 to 1.0 percent of trans-1,3-pentadiene, 0.1 to 1.0 percent of cyclopentadiene, 0.1 to 2.0 percent of cis-1,3-pentadiene, 0.1 to 8.0 percent of cyclopentene, 0.1 to 15.0 percent of cyclopentane, and the balance of C4 components.
The invention provides a beta-monoolefin-enriched C5 olefin fraction prepared by the method.
The invention provides application of the beta-monoolefin enriched C5 olefin fraction in the fields of resin synthesis and modification.
The invention obtains refined C5 fraction with optimized composition and mainly beta-olefin through super strong alkali isomerization and selective hydrogenation, can be applied to the fields of resin synthesis, modification and the like, and improves the application and economic value of crude C5 fraction such as residual C5, C5 after ether extraction and the like.
Advantageous effects
(1) In the invention, alpha-olefin in light C5 olefin is converted into beta-olefin by using a super-strong base catalyst, and impurities are removed by processes of multi-stage adsorption, extractive distillation and the like, so that the composition of components in the C5 olefin is optimized;
(2) Pd/Al modified by pretreated C5 olefin in Y, ce and Pr 2 O 3 Selective hydrogenation is carried out under the action of a catalyst, part of C5 diolefin is converted into mono-olefin, residual alkyne and sulfur nitrogen impurities in the fraction are removed, the proportion of mono-olefin in the light C5 composition is improved, and the oil product performance is improved;
(3) The invention adopts the extraction rectification process of a DMF-furfural composite solvent to complete the denitrification of C5 olefin and remove alkyne;
(4) The refined C5 fraction mainly containing beta-olefin after optimized composition can be applied to the fields of resin synthesis, modification and the like, and the application and economic value of crude C5 fractions such as residual C5 and C5 after ether extraction are improved.
Drawings
FIG. 1 is a flow diagram of a process for the preparation of a beta-monoolefin enriched C5 olefin fraction.
Detailed Description
The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and such equivalents may fall within the scope of the present invention as defined in the appended claims.
TABLE 1 typical composition (wt%) of different C5 olefins
The 4 different C5 monoolefins, wherein the raffinate C5 (a) is obtained by cracking C5 and extracting diolefins such as CPD, IP and the like; the raffinate C5 (b) is obtained after petroleum resin or curing agent is produced and cut; the high olefin C5 is an olefin enrichment component obtained by rectifying and cutting C5 after ether, and is mostly used as a synthetic resin raw material.
The following examples and comparative examples all adopt a foam porous titanium plate with an upper layer of 50 mu m and a lower layer of spherical alumina with phi 5mm by adopting an adsorption filler; the operating temperature of the packed bed is 25 ℃, and the operating pressure is 0.1MPa
Example 1
Adding the raffinate C5 (a) into a high-pressure reaction kettle with stirring in advance, and adding 0.1wt% of superbase catalyst Na-NaOH/gamma-Al under the protection of nitrogen 2 O 3 After isomerization reaction is carried out for 10min at the temperature of 0 ℃, alkaline mechanical impurities are firstly filtered out by activated clay, the pH value of the alkaline mechanical impurities is adjusted to 7.5, then the alkaline mechanical impurities are conveyed to an extraction and rectification tower, alkynes are removed by extraction and rectification under the action of a composite solvent of furfural and DMF = 2: 1, and then the alkynes enter an adsorption packed bed to remove trace water, impurities and the like, so that C5 fraction A is obtained. After the above fraction A is transferred to the hydrogenation reactor, modified by 0.1wt% Y by 0.3wt% Pd/Al 2 O 3 With H under the action of a catalyst 2 Selectively hydrogenating at 50 deg.C and 1.0MPa to obtain a product with LHSV of 10h -1 And the hydrogen-oil ratio is 50: 1, and finally the beta-olefin-enriched C5 fraction B is obtained.
The extraction and rectification operating conditions are that the solvent ratio is 0.5, the rectification reflux ratio is 2, the feeding temperature of an extraction tower is 40 ℃, the tower top temperature is 60 ℃, the tower bottom temperature is 80 ℃, and the operating pressure is 0.15MPa;
the composition of the C5 fraction A was: 0.05% of trans-2-butene, 0.10% of cis-2-pentene, 0.66% of 3-methyl-1-butene, 10.48% of isopentane, 0.52% of 1,4-pentadiene, 0.02% of 2-butyne, 7.75% of 1-pentene, 0.33% of isopentyne, 2.06% of 2-methyl-1-butene, 31.57% of n-pentane, 0.78% of isoprene, 5.72% of trans-2-pentene, 3.51% of cis-2-pentene, 0.03% of 1-pentyne, 20.25% of 2-methyl-2-butene, 0.87% of trans-1,3-pentadiene, 0.19% of cyclopentadiene, 0.55% of cis-1,3-pentadiene, 0.20% of cyclopentene, 6.17% of cyclopentane and the balance of C4-C6 components.
The composition of the C5 fraction B was: trans-2-butene 0.01%, cis-2-pentene 0.05%, 3-methyl-1-butene 0.30%, isopentane 11.06%,1,4-pentadiene 0.10%, 1-pentene 6.65%, 2-methyl-1-butene 1.12%, n-pentane 33.20%, isoprene 0.10%, trans-2-pentene 3.22%, cis-2-pentene 2.10%, 2-methyl-2-butene 18.35%, trans-1,3-pentadiene 0.13%, cyclopentadiene 0.05%, cis-1,3-pentadiene 0.12%, cyclopentene 0.31%, cyclopentane 6.19%, and the balance C4-C6 components.
From the data of the above examples, it can be seen that, after the step 1 of isomerization → adsorption → extractive distillation → adsorption process, the composition of fraction a is significantly reduced in α -olefin, increased in the content after conversion to β -olefin, and reduced in the content of impurities such as prenyne, compared to raffinate C5 (a). After the selective hydrogenation in the step 2, substantially all alkynes are saturated, most diolefins are hydrogenated and converted into mono-olefins or alkanes, and a small amount of mono-olefins are also saturated.
Example 2
Adding ether into a high-pressure reaction kettle with stirring in advance, adding 0.2wt% of superbase catalyst Na-NaOH/gamma-Al under the protection of nitrogen gas, and then adding C5 2 O 3 After isomerization reaction is carried out for 10min at the temperature of 0 ℃, alkaline mechanical impurities are firstly filtered out by activated clay, the pH value of the alkaline mechanical impurities is adjusted to 7.3, then the alkaline mechanical impurities are conveyed to an extraction and rectification tower, alkynes are removed by extraction and rectification under the action of a composite solvent of furfural and DMF = 2: 1, and then the alkynes enter an adsorption packed bed to remove trace water, impurities and the like, so that C5 fraction A is obtained. After the above fraction A was transferred to the hydrogenation reactor, was subjected to Pr modification at 0.05wt% by 0.2wt% of Pd/Al 2 O 3 With H under the action of a catalyst 2 Selectively hydrogenating at 40 deg.C under 1.0MPa for 10h LHSV -1 And the hydrogen-oil ratio is 25: 1, and finally the beta-olefin-enriched C5 fraction B is obtained.
The extraction and rectification operating conditions are that the solvent ratio is 0.5, the rectification reflux ratio is 2, the feeding temperature of an extraction tower is 40 ℃, the tower top temperature is 60 ℃, the tower bottom temperature is 80 ℃, and the operating pressure is 0.15MPa;
the composition of the C5 fraction A was: 0.01% of 1-butyne, 0.03% of trans-2-butene, 0.07% of cis-2-pentene, 0.46% of 3-methyl-1-butene, 15.80% of isopentane, 0.05% of 1,4-pentadiene, 0.01% of 2-butyne, 5.25% of 1-pentene, 0.06% of isopentene, 1.86% of 2-methyl-1-butene, 0.95% of n-pentane, 0.47% of isoprene, 15.36% of trans-2-pentene, 8.28% of cis-2-pentene, 0.05% of 1-pentyne, 23.61% of 2-methyl-2-butene, 1.52% of trans-1,3-pentadiene, 0.15% of cyclopentadiene, 0.80% of cis-1,3-pentadiene, 0.66% of cyclopentene, 0.51% of cyclopentane, and the balance of C4-C6 components.
The composition of the C5 fraction B was: trans-2-butene 0.01%, cis-2-pentene 0.01%, 3-methyl-1-butene 0.22%, isopentane 17.50%,1,4-pentadiene 0.01%, 1-pentene 3.50%, 2-methyl-1-butene 1.05%, n-pentane 2.70%, isoprene 0.10%, trans-2-pentene 12.20%, cis-2-pentene 7.05%, 2-methyl-2-butene 21.87%, trans-1,3-pentadiene 0.36%, cyclopentadiene 0.1%, cis-1,3-pentadiene 0.1%, cyclopentene 0.70%, cyclopentane 0.52%, and the balance of C4-C6 components.
From the data of the above examples, it can be seen that when the amount of superbase catalyst is increased, the α -olefin conversion rate is also increased, the β -olefin relative ratio is increased, and the alkyne removal rate is not changed much. Modification of Pd/Al on Pr 2 O 3 Under the action of the catalyst, the hydrogenation selectivity of the C5 fraction is improved, the yield of alkanes such as cyclopentane and n-pentane is reduced, and the relative ratio of beta-olefin is higher.
Comparative example 1
Adding ether into a high-pressure reaction kettle with stirring in advance, adding 0.2wt% of superbase catalyst Na-NaOH/gamma-Al under the protection of nitrogen gas, and then adding C5 2 O 3 After isomerization reaction is carried out for 10min at the temperature of 0 ℃, alkaline mechanical impurities are firstly filtered out by activated clay, the pH value of the alkaline mechanical impurities is adjusted to 7.3, then the alkaline mechanical impurities are conveyed to an extraction and rectification tower, alkynes are removed by extraction and rectification under the action of a composite solvent of furfural and DMF = 2: 1, and then the alkynes enter an adsorption packed bed to remove trace water, impurities and the like, so that C5 fraction A is obtained.
After the above fraction A was transferred to the hydrogenation reactor, was subjected to Pr modification at 0.05wt% by 0.2wt% of Pd/Al 2 O 3 With H under the action of a catalyst 2 Selective hydrogenation is carried out at 68 ℃ and 1.0MPa, LHSV is 0.5h -1 Hydrogen-oil ratio of 220: 1 to finally obtain the beta-olefin-enriched C5 fractionB。
The composition of the C5 fraction A was: 0.01% of 1-butyne, 0.03% of trans-2-butene, 0.08% of cis-2-pentene, 0.40% of 3-methyl-1-butene, 15.67% of isopentane, 0.05% of 1,4-pentadiene, 0.01% of 2-butyne, 5.25% of 1-pentene, 0.06% of isopentene, 1.80% of 2-methyl-1-butene, 0.95% of n-pentane, 0.47% of isoprene, 15.36% of trans-2-pentene, 8.28% of cis-2-pentene, 0.05% of 1-pentyne, 23.70% of 2-methyl-2-butene, 1.52% of trans-1,3-pentadiene, 0.15% of cyclopentadiene, 0.79% of cis-1,3-pentadiene, 0.67% of cyclopentene, 0.50% of cyclopentane, and the balance of C4-C6 components.
The composition of the C5 fraction B was: trans-2-butene 0.01%, cis-2-pentene 0.01%, 3-methyl-1-butene 0.08%, isopentane 26.27%,1,4-pentadiene 0.01%, 1-pentene 2.00%, 2-methyl-1-butene 0.67%, n-pentane 4.30%, isoprene 0.05%, trans-2-pentene 10.20%, cis-2-pentene 6.06%, 2-methyl-2-butene 12.73%, trans-1,3-pentadiene 0.16%, cyclopentadiene 0.05%, cis-1,3-pentadiene 0.1%, cyclopentene 0.20%, cyclopentane 1.27%, and the balance C4-C6 components.
From the comparison of the data of comparative example 1 and example 2, it can be seen that as the hydrogenation temperature, the hydrogen-oil ratio and the LHSV are increased, the hydrogenation of the olefin tends to generate the paraffin, the content of the saturated hydrocarbon such as isopentane and n-pentane in the C5 fraction B is increased, the content of the β -olefin such as 2-methyl-2-butene is greatly reduced by 9.14%, and the hydrogenation selectivity is deteriorated.
Claims (6)
1. A process for the preparation of a C5 olefin fraction enriched in β -mono-olefins, comprising:
(1) Under the protection of nitrogen, adding a catalyst into crude C5 olefin, carrying out isomerization reaction for 1-30 min at the temperature of-5-25 ℃, then adjusting the pH value to 6-8 through activated clay, then carrying out extraction rectification under the action of a composite solvent, and then entering an adsorption packed bed to obtain C5 fraction A;
(2) The C5 fraction A is subjected to modified Pd/Al 2 O 3 Under the action of a catalyst, with H 2 Selectively hydrogenating at 25-65 deg.c and 0.8-1.5 MPa and liquid hourly space velocity LHSV of 1-20 hr -1 Hydrogen to oil ratio of 1 to 200) 1 to obtain a beta-olefin enriched C5 fraction B,
the crude C5 olefin in the step (1) comprises the following components: 0 to 0.30 percent of 1-butyne, 0.01 to 0.5 percent of trans-2-butene, 0.01 to 0.8 percent of cis-2-pentene, 0.1 to 2.0 percent of 3-methyl-1-butene, 5.0 to 40.0 percent of isopentane, 0.01 to 2.0 percent of 1,4-pentadiene, 0.01 to 0.2 percent of 2-butyne, 0.5 to 10.0 percent of 1-pentene, 0.01 to 5.0 percent of isopentene, 0.5 to 20.0 percent of 2-methyl-1-butene, 0.5 to 40.0 percent of n-pentane, 0.1 to 5.0 percent of isoprene, 1.0 to 20 percent of trans-2-pentene, 1.0 to 15 percent of cis-2-pentene, 0.01 to 0.5 percent of 1-pentyne, 1.0 to 25 percent of 2-methyl-2-butene, 0.1.1 to 3.0 percent of trans-1,3-pentadiene, 0.1 to 3.63 percent of cyclopentadiene, 0.1 to 10.1 zxft, 0 to 10 percent of cyclopentane, and the balance of C components of C;
the catalyst in the step (1) is a super-strong base catalyst; the super alkali catalyst is Na-MgO, na/gamma-Al 2 O 3 、Na-NaOH/γ-Al 2 O 3 、K-KOH/γ-Al 2 O 3 、K-NaOH/γ-Al 2 O 3 、KNO 3 /γ-Al 2 O 3 One or more of the above; the addition amount of the catalyst is 0.01 to 0.5 weight percent;
the composite solvent in the step (1) is a mixed solution of furfural and DMF; wherein the mass ratio of the furfural to the DMF is (1-5) to 1; the extraction and rectification in the step (1) is specifically as follows: the solvent ratio is 0.4-0.6, the rectification reflux ratio is 2-3, the feeding temperature of an extraction tower is 35-70 ℃, the tower top temperature is 40-75 ℃, the tower kettle temperature is 60-120 ℃, and the operating pressure is 0.12-0.20 MPa;
the packing in the adsorption packed bed in the step (1) is as follows: the upper layer is a 20-60 mu m foam porous titanium plate, and the lower layer is 3-6 mm spherical alumina; the operating temperature of the packed bed is 5-40 ℃, and the operating pressure is 0.1-0.3 MPa.
2. The method according to claim 1, wherein the composition of fraction a comprises: 0 to 0.10 percent of 1-butyne, 0.01 to 0.5 percent of trans-2-butene, 0.01 to 0.8 percent of cis-2-pentene, 0.1 to 1.5 percent of 3-methyl-1-butene, 5.0 to 40.0 percent of isopentane, 0.01 to 2.0 percent of 1,4-pentadiene, 0.01 to 0.05 percent of 2-butyne, 0.5 to 10.0 percent of 1-pentene, 0.01 to 0.5 percent of isopentene, 0.1 to 10.0 percent of 2-methyl-1-butene, 0.5 to 40.0 percent of n-pentane, 0.1 to 5.0 percent of isoprene, 1.0 to 20 percent of trans-2-pentene, 1.0 to 15 percent of cis-2-pentene, 0.01 to 0.10 percent of 1-pentyne, 1.0 to 35 percent of 2-methyl-2-butene, 0.1.1 to 3.0 percent of trans-5262 zxft 0.1 to 3.63 percent of cyclopentadiene, 0.1 to 0.1 zxft, 0 to 10 percent of the rest of cyclopentane, 0.6 to 0 to 3.1 to 0 percent of C.
3. The method according to claim 1, wherein the Pd/Al is modified in the step (2) 2 O 3 The catalyst has main catalyst Pd content of 0.1-2.0 wt% and modified component Y, ce or Pr content of 0.03-1.0 wt%.
4. The method according to claim 1, wherein the composition of fraction B in step (2) comprises: 0.01 to 0.2 percent of trans-2-butene, 0.01 to 0.2 percent of cis-2-pentene, 0.1 to 1.5 percent of 3-methyl-1-butene, 5.0 to 45.0 percent of isopentane, 0.01 to 0.5 percent of 1,4-pentadiene, 0.5 to 8.0 percent of 1-pentene, 0.1 to 10.0 percent of 2-methyl-1-butene, 0.5 to 43.0 percent of n-pentane, 0.1 to 3.0 percent of isoprene, 0.5 to 15 percent of trans-2-pentene, 0.5 to 10 percent of cis-2-pentene, 1.0 to 33 percent of 2-methyl-2-butene, 0.1 to 1.0 percent of trans-1,3-pentadiene, 0.1 to 1.0 percent of cyclopentadiene, 0.1 to 2.0 percent of cis-1,3-pentadiene, 0.1 to 8.0 percent of cyclopentene, 0.1 to 15.0 percent of cyclopentane, and the balance of C4 components.
5. A beta-monoolefin enriched C5 olefin fraction prepared by the process of claim 1.
6. Use of the beta-monoolefin enriched C5 olefin fraction of claim 1 in the field of resin synthesis and modification.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1160033A (en) * | 1996-03-20 | 1997-09-24 | 中国石油化工总公司 | Method for separation of cracking C5 fraction by pre-removal process of alkyne |
| CN1412165A (en) * | 2001-10-12 | 2003-04-23 | 中国石油化工股份有限公司 | Separation method of cracked C5 fraction |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
| CN101244973A (en) * | 2007-02-15 | 2008-08-20 | 中国石油化工股份有限公司 | Method for removing alkyne in high purity isoprene |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1160033A (en) * | 1996-03-20 | 1997-09-24 | 中国石油化工总公司 | Method for separation of cracking C5 fraction by pre-removal process of alkyne |
| CN1412165A (en) * | 2001-10-12 | 2003-04-23 | 中国石油化工股份有限公司 | Separation method of cracked C5 fraction |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
| CN101244973A (en) * | 2007-02-15 | 2008-08-20 | 中国石油化工股份有限公司 | Method for removing alkyne in high purity isoprene |
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