CN109897124B - Continuous preparation device and preparation method of refined polyethylene wax - Google Patents
Continuous preparation device and preparation method of refined polyethylene wax Download PDFInfo
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- CN109897124B CN109897124B CN201910347187.5A CN201910347187A CN109897124B CN 109897124 B CN109897124 B CN 109897124B CN 201910347187 A CN201910347187 A CN 201910347187A CN 109897124 B CN109897124 B CN 109897124B
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Abstract
The invention relates to a preparation device and a preparation method of continuous refined polyethylene wax, wherein the preparation method comprises the following steps of S1: continuously conveying the solid polyethylene wax crude product and superheated steam into a stripping tower at a constant speed according to the weight ratio, and stacking the solid polyethylene wax crude product on a screen plate; s2: under the action of superheated steam, the solid polyethylene wax crude product is melted and stripped in the packing layer, and then is output and molded after being filtered by a liquid loading funnel. The method adopts the solid polyethylene wax crude product as a raw material, adopts superheated steam to melt and strip the solid polyethylene wax crude product under normal pressure, and simply and efficiently prepares the refined polyethylene wax.
Description
Technical Field
The invention relates to the technical field of polymer materials, in particular to a continuous preparation device and a preparation method of refined polyethylene wax.
Background
Polyethylene wax is a low molecular weight polyethylene copolymer with a molecular weight of about 1000-5000-. Compared with paraffin, the polyethylene wax has the characteristics of large molecular weight, large viscosity and high melting point, is mainly applied to processing polyolefin plastics to be used as a lubricant, has the main characteristics of good heat resistance and difficult precipitation, and can also be applied to hot melt adhesives and road marking paints to play the roles of reducing the construction viscosity, increasing the fluidity, improving the softening point and the like.
In the polymerization process of the polyethylene wax, due to multi-catalyst reaction centers and the like, a plurality of ethylene copolymer light components with the molecular weight of less than 300 and smaller molecular weight can be formed, the proportion of the ethylene copolymer light components is generally between 3 and 8 percent according to different polymerization conditions, and the light components play a bad role in the application of the polyethylene wax. In polyolefin plastic products, white powder is precipitated, which causes the plastic products to turn white or have reduced gloss. The softening point of the product can be influenced by hot melt adhesive and road marking paint.
The polyethylene wax is refined and purified to obtain a product with better quality, which is the requirement of industrial technology development. The invention patent 201611104973.5 filed by China oil and gas Limited company adopts a steam stripping and negative pressure high temperature dehydration mode to refine and purify polyethylene wax, the operation mode is intermittent operation, and under the premise that large petrochemical enterprises have molten polyethylene wax resources and do not need the operation of melting polyethylene wax solids, the operation time of each batch is about 20 hours, and the efficiency is low.
Disclosure of Invention
The invention aims to provide a continuous preparation device and a preparation method of refined polyethylene wax.
In order to achieve the purpose, the technical scheme of the invention is as follows:
the utility model provides a preparation facilities of continuous type refined low molecular weight polyethylene, includes steam generator, superheated steam heat exchanger, strip tower, heat exchanger, oil water separator and pump, strip tower top one side is equipped with the feed inlet, and the opposite side is equipped with the export of light component, is equipped with steam inlet on the lateral wall, through the export of light component externally connects gradually heat exchanger and oil water separator, steam generator passes through superheated steam heat exchanger and connects steam inlet, strip tower bottom is the external pump that connects.
In the scheme, the stripping tower is internally provided with the mesh plate, the packing layer and the liquid loading funnel from top to bottom in sequence.
A preparation method of continuous refined polyethylene wax is carried out by utilizing a preparation device of continuous refined polyethylene wax, and comprises the following steps:
s1: continuously conveying the solid polyethylene wax crude product and superheated steam into a stripping tower at a constant speed according to the weight ratio, and stacking the solid polyethylene wax crude product on a screen plate;
s2: under the action of superheated steam, the solid polyethylene wax crude product is melted and stripped in the packing layer, and then is output and molded after being filtered by a liquid loading funnel.
In the scheme, the temperature of the superheated steam is 160-200 ℃, and the superheat degree is not less than 30 ℃.
In the scheme, the weight ratio of the solid polyethylene wax crude product to the superheated steam is 1: 8-1: 20.
The continuous refined polyethylene wax preparation device and the preparation method directly heat the solid polyethylene wax crude product by superheated steam, and steam stripping is carried out while melting; meanwhile, the stripping tower is kept to operate at a higher temperature, so that the water content in the molten polyethylene wax is always kept at a lower equilibrium level; the solid polyethylene wax crude product is fed in a continuous mode, and the stripped polyethylene wax is continuously discharged, so that the refined polyethylene wax is simply and efficiently prepared.
Drawings
FIG. 1 is a schematic structural view of an apparatus for continuously producing a purified polyethylene wax according to one embodiment of the present invention;
description of reference numerals: 1. steam generator, 2 superheated steam heat exchanger, 3 feeding equipment, 4 heat exchanger, 5 oil water separator, 6 stripping tower, 61 screen plate, 62 packing layer, 63 effusion funnel, 7 pump.
Detailed Description
The technical solution of the present invention is further described in detail with reference to the accompanying drawings and examples.
The invention discloses a continuous refined polyethylene wax preparation device, which comprises a steam generator 1, a superheated steam heat exchanger 2, a stripping tower 6, a heat exchanger 4, an oil-water separator 5 and a pump 7, as shown in figure 1. Wherein, 6 top of the tower one side in strip tower is equipped with the feed inlet, and the opposite side is equipped with the light component export, is equipped with steam inlet on the lateral wall, connects gradually heat exchanger 4 and oil water separator 5 outward through the light component export, and steam generator 1 connects steam inlet through superheated steam heat exchanger 2, and 6 bottoms in strip tower are equipped with the discharge gate, external connection pump 7. The stripping tower 6 is internally provided with a mesh plate 61, a packing layer 62 and a liquid loading funnel 63 from top to bottom in sequence.
A preparation method of continuous refined polyethylene wax utilizes a preparation device of continuous refined polyethylene wax to carry out continuous refining, and comprises the following specific steps:
at first, use feeding equipment 3 to carry solid polyethylene wax crude product through the feed inlet of stripping tower 6, solid polyethylene wax crude product piles on otter board 61, superheated steam produced by steam generator 1 and superheated steam heat exchanger 2 passes through steam inlet and gets into stripping tower 6, melt solid polyethylene wax crude product, polyethylene wax liquid after melting strips at packing layer 62, get into the bottom of the tower through hydrops funnel 63, and make a small amount of impurity that exists in the solid polyethylene wax crude product deposit at the bottom of the tower more easily through hydrops funnel 63, the clear polyethylene wax in upper strata passes through pump 7 and exports the shaping outward. Meanwhile, residual steam and light components generated by steam stripping enter a heat exchanger 4 for condensation and then enter an oil-water separator 5 for separation treatment.
In the stripping process, the amount of the superheated steam and the weight of the crude solid polyethylene wax are continuously conveyed according to the weight ratio, the preferable weight ratio of the crude solid polyethylene wax and the superheated steam is 1: 8-1: 20, the temperature of the superheated steam is 160-200 ℃, and in order to ensure that the water content in the polyethylene wax liquid is less, the degree of superheat of the superheated steam is not less than 30 ℃.
Example 1
Adding a sheet solid polyethylene wax crude product with the light component content of 9% into a stripping tower 6 at the speed of 200kg/h, wherein a steam generator generates saturated steam at the temperature of 130 ℃, the saturated steam is heated by a hot steam heat exchanger to form superheated steam at the temperature of 200 ℃, the superheat degree is 70 ℃, the flow of the superheated steam is 1600kg/h, the continuous operation is carried out for 10 hours, and 1830kg of refined polyethylene wax A is obtained, and the yield is about 91.5%.
Example 2
Adding a sheet solid polyethylene wax crude product with the light component content of 9% into a stripping tower 6 at the speed of 200kg/h, wherein a steam generator generates saturated steam at the temperature of 130 ℃, the saturated steam is heated by a hot steam heat exchanger to form superheated steam at the temperature of 160 ℃, the superheat degree is 30 ℃, the flow of the superheated steam is 2000kg/h, the continuous operation is carried out for 10 hours, and 1880kg of refined polyethylene wax B is obtained, and the yield is about 94%.
Table 1 shows the comparative test table of the solid polyethylene wax crude product and the refined polyethylene wax:
| volatile matter | Melt drop point | Penetration degree | |
| Solid polyethylene wax crude product | 9％ | 102℃ | 12dmm |
| Refined polyethylene wax A | 2.1％ | 108℃ | 5dmm |
| Refined polyethylene wax B | 3.3％ | 106℃ | 6dmm |
And carrying out a comparative test on the raw material of the crude solid polyethylene wax product, the refined polyethylene wax A and the refined polyethylene wax B. The method for testing the melting point of the polyethylene wax adopts GB/T8026-2014 petroleum wax and petroleum fat drop melting point measurement method, the method for testing the hardness of the polyethylene wax adopts GBT 4985-2010 petroleum wax penetration measurement method, and the data in Table 1 show that the melting point of the polyethylene wax prepared by the preparation device and the preparation method is improved to a certain extent, and the smaller the penetration reading is, the higher the hardness is, and the volatile matter is obviously reduced.
The above-mentioned embodiments are intended to illustrate the technical solutions and advantages of the present invention, and it should be understood that the above-mentioned embodiments are only specific embodiments of the present invention, and are not intended to limit the present invention, and any modifications, additions, equivalents, etc. made within the scope of the principles of the present invention should be included in the scope of the present invention.
Claims (2)
1. The utility model provides a preparation facilities of continuous type refined polyethylene wax which characterized in that: the device comprises a steam generator (1), a superheated steam heat exchanger (2), a stripping tower (6), a heat exchanger (4), an oil-water separator (5) and a pump (7), wherein a feed inlet is formed in one side of the top of the stripping tower (6), a light component outlet is formed in the other side of the top of the stripping tower, a steam inlet is formed in the side wall of the stripping tower, the heat exchanger (4) and the oil-water separator (5) are sequentially connected to the outside through the light component outlet, the steam generator (1) is connected with the steam inlet through the superheated steam heat exchanger (2), and the bottom of the stripping tower (6) is connected with the pump (7) to the outside; and the stripping tower (6) is internally provided with a mesh plate (61), a packing layer (62) and a liquid loading funnel (63) from top to bottom in sequence.
2. A process for producing a continuous purified polyethylene wax which is continuously carried out by the apparatus for producing a continuous purified polyethylene wax according to claim 1, comprising the steps of:
s1: continuously conveying the solid polyethylene wax crude product and superheated steam into a stripping tower (6) at a constant speed according to the weight ratio of the solid polyethylene wax crude product to the superheated steam of 1: 8-1: 20, wherein the temperature of the superheated steam is 160-200 ℃, and the degree of superheat is not less than 30 ℃;
s2: under the action of superheated steam, the solid polyethylene wax crude product on the screen plate (61) is melted, the melted polyethylene wax liquid is stripped in the packing layer (62), and then is output and molded after being filtered by the effusion funnel (63).
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|---|---|---|---|---|
| US5141630A (en) * | 1990-03-15 | 1992-08-25 | Lyondell Petrochemical Company | Separation process employing two stripping gases |
| CN204824803U (en) * | 2015-07-07 | 2015-12-02 | 济宁学院 | Filler combination formula strip tower |
| CN105289026A (en) * | 2014-06-17 | 2016-02-03 | 上海氯碱化工股份有限公司 | Method for continuously stripping and removing residual vinyl chloride in paste resin latex |
| CN108148151A (en) * | 2016-12-05 | 2018-06-12 | 中国石油天然气股份有限公司 | The process for purification and refining plant of refined polyethylene wax, polyethylene wax crude product |
| CN108219189A (en) * | 2016-12-15 | 2018-06-29 | 中国石油天然气股份有限公司 | The method for detaching PE low molecular polymer |
| CN108671575A (en) * | 2018-06-28 | 2018-10-19 | 山西潞安纳克碳化工有限公司 | superheated steam stripping system |
-
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- 2019-04-28 CN CN201910347187.5A patent/CN109897124B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5141630A (en) * | 1990-03-15 | 1992-08-25 | Lyondell Petrochemical Company | Separation process employing two stripping gases |
| CN105289026A (en) * | 2014-06-17 | 2016-02-03 | 上海氯碱化工股份有限公司 | Method for continuously stripping and removing residual vinyl chloride in paste resin latex |
| CN204824803U (en) * | 2015-07-07 | 2015-12-02 | 济宁学院 | Filler combination formula strip tower |
| CN108148151A (en) * | 2016-12-05 | 2018-06-12 | 中国石油天然气股份有限公司 | The process for purification and refining plant of refined polyethylene wax, polyethylene wax crude product |
| CN108219189A (en) * | 2016-12-15 | 2018-06-29 | 中国石油天然气股份有限公司 | The method for detaching PE low molecular polymer |
| CN108671575A (en) * | 2018-06-28 | 2018-10-19 | 山西潞安纳克碳化工有限公司 | superheated steam stripping system |
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