CN1676500A - Method for separating alpha-butylene - Google Patents
Method for separating alpha-butylene Download PDFInfo
- Publication number
- CN1676500A CN1676500A CN 200410030737 CN200410030737A CN1676500A CN 1676500 A CN1676500 A CN 1676500A CN 200410030737 CN200410030737 CN 200410030737 CN 200410030737 A CN200410030737 A CN 200410030737A CN 1676500 A CN1676500 A CN 1676500A
- Authority
- CN
- China
- Prior art keywords
- tower
- butylene
- absorption
- temperature
- pressure
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 39
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical group CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 title description 15
- 238000010521 absorption reaction Methods 0.000 claims abstract description 80
- 239000000463 material Substances 0.000 claims abstract description 12
- -1 olefin hydrocarbon Chemical class 0.000 claims abstract description 12
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 7
- GGCZERPQGJTIQP-UHFFFAOYSA-N sodium;9,10-dioxoanthracene-2-sulfonic acid Chemical compound [Na+].C1=CC=C2C(=O)C3=CC(S(=O)(=O)O)=CC=C3C(=O)C2=C1 GGCZERPQGJTIQP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 74
- 239000007788 liquid Substances 0.000 claims description 45
- SQGYOTSLMSWVJD-UHFFFAOYSA-N silver(1+) nitrate Chemical compound [Ag+].[O-]N(=O)=O SQGYOTSLMSWVJD-UHFFFAOYSA-N 0.000 claims description 16
- 241000282326 Felis catus Species 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 13
- 238000010992 reflux Methods 0.000 claims description 11
- 229910001961 silver nitrate Inorganic materials 0.000 claims description 8
- 239000004332 silver Substances 0.000 claims description 6
- 229910052709 silver Inorganic materials 0.000 claims description 6
- IAQRGUVFOMOMEM-UHFFFAOYSA-N but-2-ene Chemical compound CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 abstract description 2
- 239000004215 Carbon black (E152) Substances 0.000 abstract 1
- 229930195733 hydrocarbon Natural products 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 53
- 239000000047 product Substances 0.000 description 28
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 8
- 239000000203 mixture Substances 0.000 description 7
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000004587 chromatography analysis Methods 0.000 description 3
- 230000000536 complexating effect Effects 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000004700 high-density polyethylene Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- 239000010935 stainless steel Substances 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 238000010668 complexation reaction Methods 0.000 description 2
- 238000006471 dimerization reaction Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 229920001903 high density polyethylene Polymers 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 239000012266 salt solution Substances 0.000 description 2
- IAQRGUVFOMOMEM-ONEGZZNKSA-N trans-but-2-ene Chemical compound C\C=C\C IAQRGUVFOMOMEM-ONEGZZNKSA-N 0.000 description 2
- 101710134784 Agnoprotein Proteins 0.000 description 1
- 229920010126 Linear Low Density Polyethylene (LLDPE) Polymers 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- FOIXSVOLVBLSDH-UHFFFAOYSA-N Silver ion Chemical compound [Ag+] FOIXSVOLVBLSDH-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 238000006266 etherification reaction Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 229920001580 isotactic polymer Polymers 0.000 description 1
- 229920004889 linear high-density polyethylene Polymers 0.000 description 1
- 229920000092 linear low density polyethylene Polymers 0.000 description 1
- 239000004707 linear low-density polyethylene Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000003348 petrochemical agent Substances 0.000 description 1
- 238000005120 petroleum cracking Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 150000003378 silver Chemical class 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
This invention discloses a method of separating alpha-butylenes. This method includes: the absorption solution containing soluble silver salt contacts raw gas containing C4 olefin hydrocarbon in absorption tower, selectively absorb alpha-butylenes and dimethylethene; lead the absorption solution containing alpha-butylenes and dimethylethene from the bottom of the tower to the analytic still to be analyzed; the gas materials analyzed in the still to be rectificated in fractionating tower, and get highly pure alpha-butylenes from top of the tower, and dimethylethene from the bottom of the tower. This invention solves the problems of too many theoretical boards, large feedback current ratio and high consumption of the present technology, and has the effects of low consumption, easy operation and stable product quality.
Description
Technical field
The present invention relates to a kind of separation method of mixed gas, specifically, the present invention relates to a kind of method of from the mixed gas that contains C 4 olefin, separating 1-butylene.
Background technology
At present, butylene is a most important basic petrochemical materials except that ethene, propylene.Butylene has four kinds of isomer, i.e. 1-butylene, suitable-2-butylene, anti--2-butylene, iso-butylene are all from the C in catalytic cracking, petroleum cracking and the Sweet natural gas of refinery
4Cut.Wherein, 1-butylene is the comonomer of linear low density polyethylene (LLDPE) and high density polyethylene(HDPE) (HDPE), be rate of increase one of petrochemicals faster in recent years, world's average annual growth rate is 14% between 1981～nineteen ninety, nineteen ninety the global output of 1-butylene reach 360,000 tons approximately.World's yearly capacity of LLDPE in 1993 has reached 1.2 * 10
4Kt accounts for 70% of polythene material overall throughput, and its demand is also in sharp increase.The poly-1-butylene of at first being developed by the Shell Oil Co. of commodity is a kind of macromolecular material, and it is to be the isotactic polymer of raw material with the high purity butene-1, and main application also can be made into film and sheet material for making tubing.According to the purposes difference, also different to the purity requirement of 1-butylene, generalized case, the purity of 1-butylene is about 95%～99.5%.
ZL94110735.3 discloses and has a kind ofly made the method for high-purity butylene-1 by the ethylene dimerization method, but because the ethylene dimerization method adopts and is worth higher ethene and makes raw material, cost is higher, generally is uneconomic.CN1355158A discloses a kind of method of utilizing sulfur-contained c 4 fraction to produce high-purity butylene-1, this method removes most of iso-butylene by etherification reaction earlier, utilize fractionation that butene-1 is separated with light, heavy carbon four components then, make sulfide content in the butene-1 product be lower than sulfide content in the raw material simultaneously, also can make to the small part butene-2 in case of necessity to be converted into butene-1 by isomerization reaction.
The butylene tripping device of domestic certain petrochemical plant, the method for employing rectifying separation, knockout tower is divided into two sections, and total stage number is 124, and reflux ratio is 42, and tower height is 71 meters, and thermal load is very high, is 5.5 * 10
6Kcal/h.This method is to adopt rectificating method that 1-butylene is separated from the mixture of butane and alkene, but because the boiling point of four kinds of isomer of butylene is close, for example the boiling point of iso-butylene and butene-1 much at one, butene-1 and butene-2 also only differ the several years, it is quite difficult adopting fractionation by distillation, energy consumption is quite high, and the performance accuracy requirement is high, causes the quality product fluctuation easily.
In sum, the method that precise distillation separates 1-butylene in the prior art exists that number of theoretical plate is many, reflux ratio is big, energy consumption is high, facility investment is big and performance accuracy requires high shortcoming, and the demand of high purity butene-1 is grown with each passing day, therefore, in order to solve the problem that exists in the existing 1-butylene isolation technique, the method that separation 1-butylene a kind of economy, easy and simple to handle is provided is very necessary.
Summary of the invention
The inventor is through deep research, the method of separation 1-butylene of the present invention has been proposed: at first adopt the absorption liquid absorption process that 1-butylene and suitable-2-butylene are separated, by rectifying 1-butylene and suitable-2-butylene are separated into 1-butylene product and suitable-2-butylene product then from the mixture of butane and monoolefine.
Concrete, the method for separation 1-butylene of the present invention may further comprise the steps:
(1) unstripped gas that contains C 4 olefin enters the absorption tower from the bottom on absorption tower, absorption liquid enters the absorption tower from the top on absorption tower, most of 1-butylene and suitable-2-butylene and a spot of other component are absorbed by liquid absorption in the absorption tower, draw the absorption liquid that is rich in 1-butylene and suitable-2-butylene from the tower still, other component that is not absorbed by liquid absorption is drawn from cat head;
(2) absorption liquid that is rich in 1-butylene and suitable-2-butylene of drawing from absorption Tata still enters the extraction-container parsing, in extraction-container 1-butylene and the suitable-2-butylene gas that absorbs is parsed; Preferably the absorption liquid recirculation after resolving enters the absorption tower;
(3) resolve the gas material that contains 1-butylene and suitable-2-butylene obtain by extraction-container and enter rectifying tower, carry out rectifying separation, obtain the 1-butylene product, obtain suitable-2-butylene product from the tower still from cat head from the middle part of rectifying tower.
Wherein said absorption liquid is the solution that contains soluble silver salt, and the mass percent concentration of silver ions is 5% to its saturation concentration.Because silver ions is bigger to the complexing coefficient of 1-butylene and these two kinds of components of suitable-2-butylene, complexing coefficient to other component is less, silver salt solution can selectivity absorbs these the two kinds of components in the unstripped gas, thereby 1-butylene and suitable-2-butylene enter and are retained in the absorption liquid and flow out with absorption liquid from the tower still in the absorption tower, and the unabsorbed 1-butylene of other component and part and suitable-2-butylene are drawn from cat head.Monovalence silver soluble ion is because of having (n-1) d
10Ns
0Electronic configuration is easily accepted electronics, easily provides too much d electronics again, and can form with unsaturated hydrocarbons such as alkene and change stable pi complex into, be the Separation by Complexation agent that suits.The silver salt that silver salt solution of the present invention uses can be inorganic silver salt, for example AgNO
3, AgClO
4, AgPF
6Also can be organic silver salts, for example hexamethylenetetramine-Yin.Preferred described absorption liquid is a silver nitrate solution, and the mass percent concentration of silver ions is 5% to 45%.
The number of theoretical plate on wherein said absorption tower is the 10-60 piece, and temperature is 5-50 ℃ in the tower, and the tower internal pressure is 0.1-2MPa, and gas-liquid inlet amount volume ratio is 1-50; The number of theoretical plate on preferred described absorption tower is the 25-50 piece, and temperature is 10-30 ℃, and pressure is 0.1-1MPa, and gas-liquid inlet amount volume ratio is 10-30.
The temperature on described absorption tower is proper in 5-50 ℃ of scope.Temperature is too high, is unfavorable for silver ion complexation carbon four components, and the treatment capacity on absorption tower is reduced, and the content of 1-butylene increases in the tail gas, so in the absorption tower the preferred 10-30 of temperature ℃.
The pressure on described absorption tower helps absorption liquid and absorbs gaseous fraction when increasing.When pressure is low,, need lower temperature, for example be controlled at below 15 ℃ in order to increase the rate of recovery of 1-butylene; When pressure improves, for example bring up to more than the 0.2MPa, temperature can adopt room temperature, further reduces thermal load.
The gas-liquid inlet amount volume ratio on described absorption tower is according to the content adjustment of 1-butylene in the unstripped gas.When the content of 1-butylene in the unstripped gas was high, the inlet amount that can suitably reduce gas improved the rate of recovery of 1-butylene as far as possible, but gas-liquid inlet amount volume ratio is too little, absorbs other carbon four components easily, made that 1-butylene content reduces in the material that enters rectifying tower; On the contrary, gas-liquid inlet amount volume ratio is too high, and the 1-butylene content in the tail gas increases, and has reduced the rate of recovery of 1-butylene.Therefore, preferred gas-liquid inlet amount volume ratio is 10-30.
The temperature of wherein said extraction-container is 30-80 ℃, and pressure is 0.05-0.3MPa.The described absorption liquid that is rich in 1-butylene and suitable-2-butylene heats in extraction-container, reduces pressure or the heating of reducing pressure etc. is separated complexing with the component that absorbs and discharged.There is no particular limitation for the operational condition of extraction-container, the condition that the C 4 olefin of absorption is parsed all can be used, for example when pressurization was adopted on the absorption tower, absorption liquid entered into extraction-container and becomes normal pressure and temperature, and the gas of absorption just spontaneously parses from absorption liquid.The temperature of industrial preferred described extraction-container is 40-70 ℃, and pressure is 0.1-0.2MPa.
Wherein said Rectification Column's Theoretical Plate Number is the 10-60 plate, and tower top temperature is 30-60 ℃, and tower top pressure is 0.3-0.8MPa, and tower still temperature is 40-80 ℃, and tower still pressure is 0.3-1.0MPa, and reflux ratio is 4-20; Preferred described Rectification Column's Theoretical Plate Number is the 15-40 plate, and tower top temperature is 35-55 ℃, and tower top pressure is 0.4-0.7MPa, and tower still temperature is 45-70 ℃, and tower still pressure is 0.4-0.8MPa, and reflux ratio is 5-10.
The unstripped gas that contains C 4 olefin that the present invention uses, the by product C-4-fraction that can be cracking petroleum hydrocarbon vapor system ethene selects hydrogenation to remove the material of diolefin, can be isolated C-4-fraction in the product that obtains of catalytic cracking, also can be the gas mixture of other carbon containing four alkane and alkene.
Because the boiling-point difference of 1-butylene and anti--2-butylene only is 0.9 ℃, 1-butylene and normal butane boiling-point difference are 5 ℃, and the boiling-point difference of 1-butylene and Trimethylmethane is 6 ℃, and the boiling-point difference of 1-butylene and suitable-2-butylene is 10 ℃; Therefore with respect to the method for separating 1-butylene in the prior art, use method of the present invention with comparalive ease 1-butylene and suitable-2-butylene to be separated.There is no particular limitation to the method for separating 1-butylene and suitable-2-butylene in the present invention, and those skilled in the art can be according to the requirement of product, and operational condition is adjusted on multiple mode ground, when for example number of theoretical plate is low, can improve reflux ratio; Can adopt pressurize, increase tower still temperature to reach isolating purpose if increase tower top temperature.Do not breaking away under the spirit of the present invention, any modification that step of the present invention (3) is made is also included within the scope of the present invention.
The method that the present invention adopts absorption and rectifying to combine is successfully separated 1-butylene, the 1-butylene product that obtains, and purity can reach 99%.Separate the method for 1-butylene with the prior art precise distillation and compare, in absorption of the present invention and analyzing step (1), (2), energy consumption is low to be clearly; In rectification step of the present invention (3), the material treatment capacity of rectifying separation significantly reduces with respect to unstripped gas on the one hand, and Rectification Column's Theoretical Plate Number and reflux ratio all reduce significantly on the other hand, so energy consumption also reduces significantly.
Therefore method of the present invention has reduced the tower height that prior art is separated the energy consumption of 1-butylene, shortened the rectifying separation tower significantly, and it is easier operate, and quality product is guaranteed, and the while by-product is suitable-the 2-butylene product.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for separation 1-butylene of the present invention.
The method of separation 1-butylene of the present invention is described particularly below in conjunction with accompanying drawing:
(1) 1 top enters absorption liquid from the absorption tower, 1 bottom enters the mixture material gas that contains C 4 olefin from the absorption tower, most of 1-butylene and suitable-2-butylene and a spot of other component are absorbed the absorption of liquid selectivity in absorption tower 1, remaining ingredient flows out from cat head, and absorption liquid flows out from the tower still;
(2) absorption liquid that is rich in 1-butylene and suitable-2-butylene that 1 tower still comes out from the absorption tower enters extraction-container 2, be heated through being heated, reducing pressure or the reducing pressure 1-butylene and the suitable-2-butylene that will absorb of the absorption liquid that is rich in 1-butylene and suitable-2-butylene in extraction-container 2 parses, and the absorption liquid recirculation after the parsing enters absorption tower 1;
(3) 1-butylene that parses and suitable-2-butylene gas material enter rectifying tower 3 from the middle part of rectifying tower 3, carry out rectifying separation, and cat head obtains the 1-butylene product, and tower still by-product is suitable-the 2-butylene product.
Embodiment
Following example will further specify method of the present invention.
Embodiment 1
Unstripped gas (component and content thereof see Table 1) enters the absorption tower that tower diameter is 20mm, the high 1m of body of the tower with the flow of 730ml/hr from the bottom of tower, filling Stainless Steel Helices in the tower, absorption liquid is the aqueous solution of Silver Nitrate, the mass percent concentration of silver nitrate solution is 30%, flow with 50ml/hr enters the absorption tower from cat head, and temperature is 10 ℃ in the tower, and pressure is 0.1MPa, tail gas is emitted from cat head, and absorption liquid flows out from the tower still;
Absorb the effusive absorption liquid of Tata still and enter extraction-container, resolve, the extraction-container temperature is 70 ℃, and pressure is 0.1MPa;
The gas that extraction-container parses (parsing gas) enters rectifying tower at the 15th block of plate of rectifying tower, and Rectification Column's Theoretical Plate Number is 30, and reflux ratio is 6, tower top temperature is 44.1 ℃, tower top pressure is 0.51MPa, and tower still temperature is 53.4 ℃, and tower still pressure is 0.53MPa.
Adopt gas chromatographic analysis unstripped gas, tail gas, parsing gas, 1-butylene product and suitable-2-butylene product, analytical results is listed in table 1.
The aluminum oxide capillary column of gas chromatography analysis method: chromatographic column: 50*0.32*0.5; Sampler temperature: 160 ℃; Column temperature: 80-180 ℃; Detector temperature: 200 ℃; Carrier gas: hydrogen, 5ml/min.
The composition of table 1 unstripped gas and product (unit: mass percent %)
| Unstripped gas | Tail gas | Resolve gas | The 1-butylene product | Suitable-the 2-butylene product | |
| Trimethylmethane | 1.46 | ?4.42 | ?0 | ?0 | ?0 |
| Normal butane | 6.11 | ?18.85 | ?0 | ?0 | ?0 |
| 1-butylene | 54.77 | ?4.02 | ?81.00 | ?99.73 | ?23.8 |
| Instead-2-butylene | 25.30 | ?75.80 | ?0.50 | ?0.08 | ?1.60 |
| Suitable-2-butylene | 12.36 | ?0.25 | ?18.50 | ?0.19 | ?74.7 |
Embodiment 2
Unstripped gas (component and content thereof see Table 2) enters the absorption tower that tower diameter is 20mm, the high 1m of body of the tower with the flow of 1350ml/hr from the bottom of tower, filling Stainless Steel Helices in the tower, absorption liquid is the aqueous solution of Silver Nitrate, the mass percent concentration of silver nitrate solution is 40%, flow with 50ml/hr enters the absorption tower from cat head, and temperature is 45 ℃ in the tower, and pressure is 0.1MPa, tail gas is emitted from cat head, and absorption liquid flows out from the tower still;
Absorb the effusive absorption liquid of Tata still and enter extraction-container, resolve, the extraction-container temperature is 70 ℃, and pressure is 0.1MPa;
The gas that extraction-container parses (parsing gas) enters rectifying tower from the 10th block of plate of rectifying tower, and Rectification Column's Theoretical Plate Number is 20, and reflux ratio is 8, tower top temperature is 44.3 ℃, tower top pressure is 0.51MPa, and tower still temperature is 51.4 ℃, and tower still pressure is 0.53MPa.
Adopt gas chromatographic analysis unstripped gas, tail gas, parsing gas, 1-butylene product and suitable-2-butylene product, analytical results is listed in table 2.
The composition of table 2 unstripped gas and product (unit: mass percent %)
| Unstripped gas | Tail gas | Resolve gas | The 1-butylene product | Suitable-the 2-butylene product | |
| Trimethylmethane | 1.46 | ?1.48 | ?0 | ?0 | ?0 |
| Normal butane | 6.11 | ?6.30 | ?0 | ?0 | ?0 |
| 1-butylene | 54.77 | ?49.82 | ?82.8 | ?99.35 | ?38.9 |
| Instead-2-butylene | 25.30 | ?29.00 | ?3.90 | ?0.21 | ?11.2 |
| Suitable-2-butylene | 12.36 | ?13.40 | ?13.30 | ?0.44 | ?49.9 |
Embodiment 3
Unstripped gas (component and content thereof see Table 3) enters the absorption tower that tower diameter is 20mm, the high 1m of body of the tower with the flow of 730ml/hr from the bottom of tower, filling Stainless Steel Helices in the tower, absorption liquid is the aqueous solution of Silver Nitrate, the mass percent concentration of silver nitrate solution is 30%, flow with 50ml/hr enters the absorption tower from cat head, and temperature is 29 ℃ in the tower, and pressure is 0.5MPa, tail gas is emitted from cat head, and absorption liquid flows out from the tower still;
Absorb the effusive absorption liquid of Tata still and enter extraction-container, resolve, the extraction-container temperature is 60 ℃, and pressure is 0.1MPa;
The gas that extraction-container parses (parsing gas) enters rectifying tower from the 15th block of plate of rectifying tower, and Rectification Column's Theoretical Plate Number is 30, and reflux ratio is 6, tower top temperature is 44.1 ℃, tower top pressure is 0.51MPa, and tower still temperature is 52.5 ℃, and tower still pressure is 0.53MPa.
Adopt gas chromatographic analysis unstripped gas, tail gas, parsing gas, 1-butylene product and suitable-2-butylene product, analytical results is listed in table 3.
The composition of table 3 unstripped gas and product (unit: mass percent %)
| Unstripped gas | Tail gas | Resolve gas | The 1-butylene product | Suitable-the 2-butylene product | |
| Trimethylmethane | 1.46 | ? ?24.65 | ?0 | ?0 | ?0 |
| Normal butane | 6.11 | ?0 | ?0 | ?0 | |
| 1-butylene | 54.77 | ?0.73 | ?82.5 | ?99.25 | ?30.4 |
| Instead-2-butylene | 25.30 | ?74.25 | ?2.50 | ?0.29 | ?8.2 |
| Suitable-2-butylene | 12.36 | Little | 15.50 | ?0.46 | ?61.4 |
Claims (10)
1. a method of separating 1-butylene is characterized in that, this method may further comprise the steps:
(1) unstripped gas that contains C 4 olefin enters the absorption tower from the bottom on absorption tower, and absorption liquid enters the absorption tower from the top on absorption tower, draws the absorption liquid that is rich in 1-butylene and suitable-2-butylene from the tower still, and other component that is not absorbed by liquid absorption is drawn from cat head;
(2) absorption liquid that is rich in 1-butylene and suitable-2-butylene of drawing from absorption Tata still enters the extraction-container parsing;
(3) resolve the gas material that contains 1-butylene and suitable-2-butylene obtain by extraction-container and enter rectifying tower, carry out rectifying separation, obtain the 1-butylene product, obtain suitable-2-butylene product from the tower still from cat head from the middle part of rectifying tower.
2. method according to claim 1 is characterized in that, described absorption liquid is the solution that contains soluble silver salt, and the mass percent concentration of silver ions is 5% to its saturation concentration.
3. method according to claim 2 is characterized in that, described absorption liquid is a silver nitrate solution, and the mass percent concentration of silver ions is 5% to 45%.
4. method according to claim 1 is characterized in that, the number of theoretical plate on described absorption tower is the 10-60 piece, and temperature is 5-50 ℃ in the tower, and the tower internal pressure is 0.1-2MPa, and gas-liquid inlet amount volume ratio is 1-50.
5, method according to claim 4 is characterized in that, the number of theoretical plate on described absorption tower is the 25-50 piece, and temperature is 10-30 ℃ in the tower, and pressure is 0.1-1MPa, and gas-liquid inlet amount volume ratio is 10-30.
6. method according to claim 1 is characterized in that, described absorption liquid recirculation after Analytic Tower is resolved enters the absorption tower.
7. method according to claim 1 is characterized in that, the temperature of described extraction-container is 30-80 ℃, and pressure is 0.05-0.3MPa.
8. method according to claim 7 is characterized in that, the temperature of described extraction-container is 40-70 ℃, and pressure is 0.1-0.2MPa.
9. method according to claim 1 is characterized in that, described Rectification Column's Theoretical Plate Number is the 10-60 plate, tower top temperature is 30-60 ℃, and tower top pressure is 0.3-0.8MPa, and tower still temperature is 40-80 ℃, tower still pressure is 0.3-1.0MPa, and reflux ratio is 4-20.
10, method according to claim 9 is characterized in that, described Rectification Column's Theoretical Plate Number is the 15-40 plate, tower top temperature is 35-55 ℃, and tower top pressure is 0.4-0.7MPa, and tower still temperature is 45-70 ℃, tower still pressure is 0.4-0.8MPa, and reflux ratio is 5-10.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410030737 CN1267389C (en) | 2004-04-02 | 2004-04-02 | Method for separating alpha-butylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410030737 CN1267389C (en) | 2004-04-02 | 2004-04-02 | Method for separating alpha-butylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1676500A true CN1676500A (en) | 2005-10-05 |
| CN1267389C CN1267389C (en) | 2006-08-02 |
Family
ID=35049263
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410030737 Expired - Lifetime CN1267389C (en) | 2004-04-02 | 2004-04-02 | Method for separating alpha-butylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1267389C (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101605873A (en) * | 2006-12-28 | 2009-12-16 | 环球油品有限责任公司 | From mixed C 4The apparatus and method of separating 1-butylene in the charging |
| US20090323385A1 (en) * | 2008-06-30 | 2009-12-31 | ScanDisk 3D LLC | Method for fabricating high density pillar structures by double patterning using positive photoresist |
| CN102040449A (en) * | 2009-10-20 | 2011-05-04 | 中国石油化工股份有限公司 | Method for separating 1-butylene |
| CN104557383A (en) * | 2013-10-10 | 2015-04-29 | 湖南中创化工股份有限公司 | Method for separating butane and butylene by using silver salt dissolved and/or dispersed organic solvent |
| CN104557391A (en) * | 2013-10-10 | 2015-04-29 | 湖南中创化工股份有限公司 | Method having solvent recovery system and used for separating butane and butylene by using silver salt dissolved and/or dispersed acetonitrile solvent |
| JP2019019086A (en) * | 2017-07-18 | 2019-02-07 | 旭化成株式会社 | Refining method of olefin |
| CN114456029A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Method and apparatus for producing 1-butene from tetracarbon |
-
2004
- 2004-04-02 CN CN 200410030737 patent/CN1267389C/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101605873A (en) * | 2006-12-28 | 2009-12-16 | 环球油品有限责任公司 | From mixed C 4The apparatus and method of separating 1-butylene in the charging |
| CN101605873B (en) * | 2006-12-28 | 2014-02-26 | 环球油品有限责任公司 | Apparatuses and methods for separating butene-1 from a mixed c4 feed |
| US20090323385A1 (en) * | 2008-06-30 | 2009-12-31 | ScanDisk 3D LLC | Method for fabricating high density pillar structures by double patterning using positive photoresist |
| CN102077346A (en) * | 2008-06-30 | 2011-05-25 | 桑迪士克3D公司 | Method for fabricating high density pillar structures by double patterning using positive photoresist |
| CN102077346B (en) * | 2008-06-30 | 2013-05-01 | 桑迪士克3D公司 | Method for fabricating high density pillar structures by double patterning using positive photoresist |
| CN102040449A (en) * | 2009-10-20 | 2011-05-04 | 中国石油化工股份有限公司 | Method for separating 1-butylene |
| CN104557383A (en) * | 2013-10-10 | 2015-04-29 | 湖南中创化工股份有限公司 | Method for separating butane and butylene by using silver salt dissolved and/or dispersed organic solvent |
| CN104557391A (en) * | 2013-10-10 | 2015-04-29 | 湖南中创化工股份有限公司 | Method having solvent recovery system and used for separating butane and butylene by using silver salt dissolved and/or dispersed acetonitrile solvent |
| JP2019019086A (en) * | 2017-07-18 | 2019-02-07 | 旭化成株式会社 | Refining method of olefin |
| CN114456029A (en) * | 2020-10-21 | 2022-05-10 | 中国石油化工股份有限公司 | Method and apparatus for producing 1-butene from tetracarbon |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1267389C (en) | 2006-08-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101475429B (en) | Method for comprehensive utilization of cracking C4 | |
| CN1285707C (en) | Naphtha optimized utilization method | |
| CN105585411A (en) | Hydrogenation method of butadiene extraction tail gas | |
| CN109627137B (en) | A kind of separation method for coal base Fischer-Tropsch olefins | |
| CN101544532B (en) | Method for producing butylene-1 by utilizing catalytic cracking by-product C4 hydrocarbons and ethylene cracking by-product C4 hydrocarbons as raw materials | |
| CN106381168A (en) | Catalytic gasoline desulfurization method capable of satisfying maximum light gasoline etherification olefin reduction demands | |
| KR101914966B1 (en) | Paraffin production method and paraffin production device | |
| CN1267389C (en) | Method for separating alpha-butylene | |
| CN105367368A (en) | Method for preparing high-purity isobutene from C_4 hydrocarbon | |
| CN103664458A (en) | Selective hydrogenation method of crude isopentene | |
| CN1148337C (en) | Process for preparing isopentene containing high content of 2-methyl-2-butene from methyl tertiary amyl ether | |
| CN1472284A (en) | Method for separating and refining etherification material from catalytic cracking gasoline | |
| TWI605868B (en) | Treatment of alcohols | |
| CN101759537A (en) | Method for producing HPLC-grade acetone | |
| CN106478337A (en) | A kind of detached method of C4 olefin/paraffin | |
| CN103664457A (en) | Selective hydrogenation method of crude isopentene | |
| CN101723791B (en) | Method for enriching mesitylene from C9 aromatics | |
| CN1267388C (en) | Method for separating n-alkane from C5 to C6 alkane isomerized products | |
| CN106478352A (en) | A kind of method producing high-purity isobutylene | |
| CN102701895B (en) | Method for extracting and separating liquid olefin and alkane mixture by adopting functional ionic liquid | |
| CN101550066B (en) | Production method of aerosol grade dimethyl ether | |
| CN108779399B (en) | Process and catalyst for producing high octane components | |
| CN116836035A (en) | Method and system for separating and purifying 1-hexene, 1-heptene and 1-octene from hydrocarbon-containing stream | |
| CN1659125A (en) | Process and apparatus for catalytic distillations | |
| CN1065266C (en) | Efficient tower-less gas fractionation technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20060802 |