CN104030872B - A kind of method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield - Google Patents
A kind of method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield Download PDFInfo
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- CN104030872B CN104030872B CN201310068348.XA CN201310068348A CN104030872B CN 104030872 B CN104030872 B CN 104030872B CN 201310068348 A CN201310068348 A CN 201310068348A CN 104030872 B CN104030872 B CN 104030872B
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- alkynes
- butene
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Abstract
The invention discloses a kind of method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield, method comprises: be dissolved with C
4the acetonitrile solvent of alkynes enters in the middle part of alkynes flashing tower, from the residue C of MTBE/ butene-1 device
4alkynes flashing tower top is entered, the C containing vinylacetylene as carrier gas
4alkynes gas flashes off in alkynes flashing tower, discharges after cooling from return tank top with non-condensable gas form; Residue C
4for deisobutanizer top gas body, deisobutanizer top non-condensable gas, butene-1 rectifying tower reactor C
4one or more.The present invention can make acetonitrile method 1,3-butadiene extraction unit raffinate product yield is absolutely simultaneously, the operation of device is not affected, thus greatly increase the economic benefit of butadiene product equipment and downstream MTBE-butene-1 device, and the vinylacetylene concentration in C4 alkynes is reduced further, improves the security of butadiene extraction unit.
Description
Technical field
The present invention relates to cracking of ethylene C
4fraction separation technology field, furtherly, relates to a kind of method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield.
Background technology
At present, for the mixed C of ethylene cracker by-product
4the utilization of cut, polar solvent is normally utilized to carry out extracting rectifying to it and in conjunction with the mode of conventional distillation to 1,3-butadiene component carries out 1 of extracting production polymerization-grade, 3-product butadiene, DMF method, acetonitrile method and NMP method respectively, containing a large amount of iso-butylenes and butene-1 component in the byproduct raffinate that 1,3-butadiene extraction plant is separated, therefore raffinate generally produces MTBE and butene-1 product as the raw materials for production of downstream MTBE/ butene-1 device.Wherein in acetonitrile method 1,3-butadiene extraction plant, C
4alkynes flashes off in alkynes flashing tower, after cooling and condensation, send battery limit (BL) as liquefied fuel.Due to C
4vinylacetylene chemical property in alkynes is active, unstable, be subject to thermopolymerization and explosive decomposition, for safety, the raffinate of the first extracting rectifying tower top is normally utilized to be incorporated into alkynes flash distillation tower top top as carrier gas in operating process, by vinylacetylene concentration dilution to 40%(weight ratio) below, yield like this as the iso-butylene in downstream unit raw materials for production raffinate and butene-1 just has certain loss, especially works as C
4when vinylacetylene in raw material is dense, raffinate product loss is just large, namely the loss of iso-butylene and butene-1 is larger, along with more and more stricter to vinylacetylene security control requirements in present butadiene extraction unit production process, require that vinylacetylene concentration must be diluted to 30%(weight ratio) below, the amount of the raffinate of such loss is increasing, and namely the yield losses of iso-butylene and butene-1 is increasing, particularly works as C
4iso-butylene in raw material and butene-1 content very high time, its loss is obvious about all the more.Along with the continuous expansion of now newly-built 1,3-butadiene extraction plant scale, the loss of its raffinate product is just obvious all the more, this reduces the economic benefit of butadiene product equipment and downstream unit.Therefore, the technology how improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield is particularly important.
Summary of the invention
For solving problems of the prior art, the invention provides a kind of method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield.The present invention can make acetonitrile method 1,3-butadiene extraction unit raffinate product yield is absolutely simultaneously, the operation of device is not affected, thus greatly increase the economic benefit of butadiene product equipment and downstream MTBE-butene-1 device, operation can be introduced more residue C4 simultaneously, vinylacetylene concentration in C4 alkynes is reduced, thus the processing safety of butadiene product equipment is greatly improved.
The object of this invention is to provide a kind of method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield.
Comprise:
Be dissolved with C
4the acetonitrile solvent of alkynes enters in the middle part of alkynes flashing tower, from the residue C of MTBE/ butene-1 device
4alkynes flashing tower top is entered, the C containing vinylacetylene as carrier gas
4alkynes gas flashes off in alkynes flashing tower, discharges after cooling from return tank top with non-condensable gas form;
The residue C of described MTBE/ butene-1 device
4for deisobutanizer top gas body, deisobutanizer top non-condensable gas, butene-1 rectifying tower reactor C
4one or more.
Described alkynes flashing tower number of theoretical plate is 5 ~ 20; Alkynes flashing tower bottom temperature is 80 ~ 120 DEG C, and pressure is 0.01 ~ 0.04MPaG, total reflux.
Residue C
4with C
4the weight ratio of alkynes medium vinyl acetylene is the bigger the better theoretically, but in actually operating, considers operability and the economy of device, be generally 2 ~ 5, and preferably 2 ~ 3.
Be dissolved with C
4the acetonitrile solvent of alkynes enters in the middle part of alkynes flashing tower, introduces the residue C of one MTBE/ butene-1 device
4the raffinate of an extraction system tower top is replaced to enter alkynes flashing tower top as carrier gas, the C containing vinylacetylene
4alkynes gas flashes off in alkynes flashing tower, and discharge from return tank after cooling, tower operates under certain stage number and processing condition, controls residue C
4flow make C
4alkynes gas medium vinyl acetylene concentration in 30%(weight ratio) below.Introduce residue C
4except improving except raffinate product yield because replacing raffinate, be exactly because the later use of residue C4 is worth not high in addition, residue C4 can be drawn more like this and dilute C4 alkynes, thus reduce the risk of explosion of C4 alkynes gas, and then improve the security of device operation.
Product yield in the present invention in raffinate is absolutely.
The present invention is by introducing the residue C of one MTBE/ butene-1 device
4replace acetonitrile method 1,3-butadiene extraction unit one extracts the method for raffinate as the carrier gas of vinylacetylene of system tower top, make butadiene extraction unit raffinate product yield for a hundred per cent, thus improve the economic benefit of butadiene product equipment and downstream MTBE/ butene-1 device, operation can be introduced more residue C4 simultaneously, vinylacetylene concentration in C4 alkynes is reduced, thus the processing safety of butadiene product equipment is greatly improved.
Accompanying drawing explanation
The method flow schematic diagram of Fig. 1 raising acetonitrile method of the present invention 1,3-butadiene extraction plant raffinate product yield
Description of reference numerals:
2-MTBE/ butene-1 device, 4-remains C
4, 5-is dissolved with C
4the acetonitrile solvent of alkynes, 6-alkynes flashing tower, 7-reflux pump, the discharging of 8-tower reactor, 9-water cooler, 10-C
4alkynes gas, 11-return tank
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
Be dissolved with C
4the acetonitrile solvent of alkynes enters in the middle part of the second stripping tower, introduces the residue C of one MTBE/ butene-1 device
4the raffinate of an extraction system tower top is replaced to enter the second stripping tower top as carrier gas, the C containing vinylacetylene
4alkynes gas stripping in alkynes flashing tower out, is discharged from return tank after cooling, controls residue C
4flow make C
4alkynes gas medium vinyl acetylene concentration in 30%(weight ratio) below.
Be dissolved with C
4the acetonitrile solvent of alkynes is 36684.8kg/h, and wherein vinylacetylene concentration is 1.493wt%;
Residue C
4the C of the butene-1 rectifying tower-I tower reactor of MTBE/ butene-1 device
4;
Second stripping tower number of theoretical plate is 10;
Second stripping tower bottom temperature is 93.4 DEG C, and pressure is 0.02MPaG, total reflux.
Residue C
4with C
4the weight ratio of alkynes gas medium vinyl acetylene is 2.69.
Each logistics composition is in table 1.
Table 1
| Logistics number | Raffinate | 4 | 5 | 10 | 8 |
| Flow kg/h | 820.0 | 820.0 | 36684.8 | 1600.0 | 35904.8 |
| Component | %wt | %wt | %wt | %wt | %wt |
| Water | 2.085 | 0.000 | 9.240 | 1.746 | 9.411 |
| C 3 | 0.087 | 0.000 | 0.000 | 0.045 | 0.000 |
| Propine | 0.000 | 0.000 | 0.000 | 0.003 | 0.000 |
| Trimethylmethane | 2.317 | 9.600 | 0.000 | 1.188 | 0.000 |
| Normal butane | 5.133 | 31.000 | 0.000 | 2.631 | 0.000 |
| Iso-butylene | 42.932 | 0.000 | 0.000 | 22.003 | 0.000 |
| Butene-1 | 29.625 | 4.500 | 0.000 | 15.183 | 0.000 |
| Anti-butene-2 | 10.079 | 35.850 | 0.000 | 5.165 | 0.000 |
| Maleic-2 | 5.742 | 19.050 | 0.000 | 2.944 | 0.000 |
| 1,3-butadiene | 0.000 | 0.000 | 0.274 | 4.896 | 0.061 |
| 1，2-butadiene | 0.000 | 0.000 | 0.017 | 0.301 | 0.004 |
| Ethylacetylene | 0.000 | 0.000 | 0.410 | 5.630 | 0.168 |
| Vinylacetylene | 0.000 | 0.000 | 1.493 | 19.861 | 0.640 |
| C 5 | 0.000 | 0.000 | 0.601 | 9.080 | 0.209 |
| Acetonitrile | 2.000 | 0.000 | 87.491 | 9.325 | 89.022 |
| Propadiene | 0.000 | 0.000 | 0.000 | 0.000 | 0.000 |
| Dipolymer | 0.000 | 0.000 | 0.474 | 0.000 | 0.484 |
| Total | 100.00 | 100.00 | 100.00 | 100.00 | 100.00 |
As seen from the above table, the iso-butylene in raffinate and butene-1 concentration all very high, in order to make C
4vinylacetylene concentration in alkynes gas reaches 19.05%(and is less than 30%) below, if the use raffinate is conventionally as carrier gas, the amount of the raffinate then needed is 820kg/h, namely palpus loss 820kg/h raffinate per hour, the present embodiment introduces one residue C4(820kg/h from MTBE/ butene-1) replace raffinate, 820kg raffinate is saved like this with regard to per hour, make raffinate product yield for a hundred per cent, thus the economic benefit of butadiene product equipment and downstream MTBE/ butene-1 device is greatly improved, in addition because the concentration of vinylacetylene has been reduced to less than 30%, the security of device operation is greatly improved.
Claims (3)
1. improve a method for acetonitrile method 1,3-butadiene extraction plant raffinate product yield, it is characterized in that described method comprises:
Be dissolved with C
4the acetonitrile solvent of alkynes enters in the middle part of alkynes flashing tower, from the residue C of MTBE/ butene-1 device
4alkynes flashing tower top is entered, the C containing vinylacetylene as carrier gas
4alkynes gas flashes off in alkynes flashing tower, discharges after cooling from return tank top with non-condensable gas form;
The residue C of described MTBE/ butene-1 device
4for deisobutanizer top gas body, deisobutanizer top non-condensable gas, butene-1 rectifying tower reactor C
4one or more; Described residue C
4with C
4the weight ratio of alkynes medium vinyl acetylene is 2 ~ 5.
2. the method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield as claimed in claim 1, is characterized in that:
Described alkynes flashing tower number of theoretical plate is 5 ~ 20; Alkynes flashing tower bottom temperature is 80 ~ 120 DEG C, and pressure is 0.01 ~ 0.04MPaG, total reflux.
3. the method improving acetonitrile method 1,3-butadiene extraction plant raffinate product yield as claimed in claim 1, is characterized in that:
Described residue C
4with C
4the weight ratio of alkynes medium vinyl acetylene is 2 ~ 3.
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| CN101555197A (en) * | 2008-04-11 | 2009-10-14 | 中国石油化工股份有限公司 | Comprehensive use method of mixed C-4 |
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| CN101555197A (en) * | 2008-04-11 | 2009-10-14 | 中国石油化工股份有限公司 | Comprehensive use method of mixed C-4 |
Non-Patent Citations (2)
| Title |
|---|
| 丁二烯抽提技术的比较和分析;张爱民;《石油化工》;20061231;第35卷(第10期);907-918 * |
| 乙腈法抽提丁二烯侧线脱炔烃技术的改进;李日祥;《石化技术》;19981231;第5卷(第4期);201-205 * |
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