CN1600756A - High-grade alpha-olefin polymerization monomer refining treatment method and device - Google Patents
High-grade alpha-olefin polymerization monomer refining treatment method and device Download PDFInfo
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- CN1600756A CN1600756A CN 03134882 CN03134882A CN1600756A CN 1600756 A CN1600756 A CN 1600756A CN 03134882 CN03134882 CN 03134882 CN 03134882 A CN03134882 A CN 03134882A CN 1600756 A CN1600756 A CN 1600756A
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- 238000006116 polymerization reaction Methods 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000004711 α-olefin Substances 0.000 title claims abstract description 25
- 239000000178 monomer Substances 0.000 title claims abstract description 24
- 238000007670 refining Methods 0.000 title claims abstract description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 103
- 239000002808 molecular sieve Substances 0.000 claims abstract description 97
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 93
- 238000001179 sorption measurement Methods 0.000 claims abstract description 84
- 239000002994 raw material Substances 0.000 claims abstract description 57
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 54
- 238000003860 storage Methods 0.000 claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 229960005419 nitrogen Drugs 0.000 claims description 54
- 238000004886 process control Methods 0.000 claims description 34
- 238000000746 purification Methods 0.000 claims description 9
- 230000001172 regenerating effect Effects 0.000 claims description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 229910052700 potassium Inorganic materials 0.000 claims description 4
- 239000011591 potassium Substances 0.000 claims description 4
- 238000007664 blowing Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 238000003556 assay Methods 0.000 claims description 2
- 239000004615 ingredient Substances 0.000 claims description 2
- 230000008929 regeneration Effects 0.000 abstract description 13
- 238000011069 regeneration method Methods 0.000 abstract description 13
- 239000012535 impurity Substances 0.000 abstract description 7
- 230000018044 dehydration Effects 0.000 abstract description 3
- 238000006297 dehydration reaction Methods 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 description 9
- 150000001336 alkenes Chemical class 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000000622 liquid--liquid extraction Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 238000000638 solvent extraction Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- OUUQCZGPVNCOIJ-UHFFFAOYSA-M Superoxide Chemical compound [O-][O] OUUQCZGPVNCOIJ-UHFFFAOYSA-M 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 1
- 238000010533 azeotropic distillation Methods 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012994 industrial processing Methods 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 210000005239 tubule Anatomy 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Drying Of Gases (AREA)
Abstract
The invention relates to a refining treatment method and a refining treatment device of a high-grade alpha-olefin polymerization monomer for reducing drag of a pipeline oil product. In the environment isolated from air, the high-grade alpha-olefin polymerization monomer liquid is pressed into a group of molecular sieve adsorption columns from bottom to top from a raw material storage tank 50 by normal-temperature nitrogen at the speed of 0.05-0.1 m/s, and the high-grade alpha-olefin polymerization monomer liquid is stored in a refined raw material storage tank 40 after being detected to be qualified by a trace moisture tester 35. The molecular sieve adsorption column can be heated to 350-400 ℃ by a nitrogen heater 34, the pressure is 2 atmospheres, the molecular sieve adsorption column is conveyed into the molecular sieve adsorption column, the outlet temperature of the molecular sieve adsorption column is kept for 2-3 hours after reaching 120 ℃, nitrogen conveying is stopped, and the molecular sieve adsorption column is naturally cooled to be regenerated. The method is simple and convenient, the device is simple, the operation process is flexible, the molecular sieve has more adsorption objects, the adsorption capacity is large, the quality of dehydration and impurity removal is good, the efficiency is high, the molecular sieve can be repeatedly regenerated and used, the regeneration treatment is simple, and the treatment cost is low.
Description
Technical field
The present invention is fine purification treatment process and the device that is used for the high alpha-olefin polymerization single polymerization monomer of oil product through pipelines drag reduction.Relate to vitochemical general method and device and tubing system field.
Background technology
High alpha-olefin also claims high carbon number alkene (higher olefins), means to contain 5 above carbon atoms and 1 aliphatic hydrocarbon at the carbon-to-carbon double bond of molecular chain-end in the molecule, is colourless liquid, and its general formula is C
nH
2nBe mainly used in the polymkeric substance of synthesizing super high molecular weight on petroleum industry, promptly flow improver (DragReducing-agent) is applied to oil product pipeline drag reduction.The general purity of its industrial polymer raw is 95～97%, in addition, contains impurity such as the moisture of 60～150ppm and trace oxygen, superoxide, carbon monoxide, carbonic acid gas, low-carbon alkene.These impurity especially moisture and oxygenatedchemicals have a significant impact the polymerisate quality, and the refinement treatment that must carry out raw material before carrying out polyreaction to be obtaining purified polymerization single polymerization monomer, thereby obtain ideal ultra-high molecular weight comb-shaped polymer.
Existing industrial chemicals fine purification treatment process has at present:
(1) chemical reaction method-with MAGNESIUM METAL or sodium
Be mainly used in the laboratory.
Realize industrialized unit, reliable measure is taked in the reply safety operation.
The production operation expense is big, the comprehensive cost height.
(2) azeotropic distillation-usefulness benzene is as entrainer
Be a kind of sophisticated industrial dehydration technique, but can not be used to take off minor amount of water.
Production equipment is complicated, easy to operate and control.
In actual production, process cost is bigger.
(3) membrane separation technique one is used solid film
Be a kind of modern technique, be applied in a lot of fields.
The key of this technology is the selection and the manufacturing of solid film.
Need do systematic study to removing minor amount of water.
(4) liquid-liquid extraction method one is used liquid extractant
Be a kind of sophisticated industrial separation technology, and be widely used.
In process of production, easy to operate and control, but process cost is big.
(5) adsorption method of separation one liquid or solid sorbent material
Be a kind of sophisticated industrial separation technology, and be used widely.
Production technique and equipment are simpler, easy to operate and control.
According to the requirement of polyreaction, be below 1ppm with moisture removal, and remove other trace impurity, have certain difficulty technically.Experimental study shows that azeotropic distillation and liquid-liquid extraction method can't satisfy so high technical requirements; Adopt chemical reaction method can satisfy technical requirements, but abnormally dangerous, be unsuitable for industrial application.The industrial processing that is mainly used in gas raw material at present of membrane separation technique and adsorption method of separation, Shang Weiyou is applied to the refinement treatment of liquid industrial raw material.In addition, emerging a kind of molecular sieve treatment technology has many good qualities at present, but only is applied to the solid absorption of empty branch and the industry of gas alkene, is not applied to the absorption of the moisture and the impurity of liquid olefin industry.
Summary of the invention
The objective of the invention is to invent that a kind of high alpha-olefin polymerization single polymerization monomer refinement treatment efficient height, treatment capacity are big, many, the renewable uses of absorption object, application is easy and expense is cheap molecular sieve adsorption method and device.
The present invention has made full use of the characteristics of molecular sieve adsorption technology, proposes and realized being applied to the method and the device of liquid olefin class feed purification processing treatment.The method of its realization is to be stored in refining raw material storage tank after in the environment of secluding air the high alpha-olefin polymerization single polymerization monomer solution from bottom to top being sent into one group of molecular sieve adsorption column from raw material storage tank.Concrete is exactly with raw material storage tank, molecular sieve adsorption post group, refining raw material storage tank and after connecting air in their pipeline and blowing off with nitrogen, to inject the high alpha-olefin polymerization single polymerization monomer solution of raw material storage filling with normal temperature nitrogen and from bottom to top press through one group of molecular sieve adsorption column, and send into refining raw material storage tank through after the assay was approved with the flow velocity of 0.05～0.10m/s.According to the quality and the treatment capacity requirement of refinement treatment, the molecular sieve adsorption post can be single-column or twin columns (parallel connection) or twin columns (parallel connection) series connection or four kinds of forms of three posts (parallel connection) series connection.If treatment capacity is especially big certainly, can also be four posts (parallel connection) series connection or more.In general, molecular sieve adsorption post just can satisfy the requirement of quality substantially, can be with the requirement that reaches of moisture in the raw material and impurity absorption, but, adopt two placed in-line methods in order to reach requirement steadily.Parallel connection then is for adding high throughput.According to the size of turnout, can select the method for single-column, twin columns or three post parallel connections for use.Be the molecular sieve of various models on the used molecular sieve principle, but be best that its chemical ingredients is 0.66K with potassium A type 3A molecular sieve
2O034Na
2OAl
2O
32.0SiO
24.5H
2O.This is owing to exist two keys in the high alpha-olefin structure, to select the principles and requirements of molecular sieve make it that self-polymeric reaction very easily take place, so should be no self-polymeric reaction, loading capacity is big, ultimate compression strength is high, long service life, abrasion fall, and powder is little, the energy consumption of regenerating is low and Technological Economy is excellent.By this principle, potassium A type 3A molecular sieve performance is optimum and alkene can not be entered in the molecule sieve aperture.This molecular sieve is that (φ 3～5mm), bulk density 0.5～0.5 5g/cm for white or canescence, blush powder or spheroidal particle
3(powder), 0.7～0.8kg/L (finished product type).The about 0.3mL/g of pore volume, the about 800m of specific surface area
2/ g, aperture 0.32nm, 750～800 ℃ of lattice damage temperature.Owing to molecular sieve in use along with the growth of time can make some obstruction of molecule sieve aperture lose efficacy.For molecular sieve can be reused, the regenerating molecular sieve treatment scheme should be arranged.When recording Moisture high UCL by online micro-moisture tester, stop liquor charging, normal temperature nitrogen directly is pressed into each molecular sieve adsorption post expel liquid with 2 atmospheric pressure, after with 350～400 ℃, pressure still is that 2 atmospheric nitrogen are sent into the molecular sieve adsorption post again, keeps 2～3 hours after molecular sieve adsorption column outlet nitrogen temperature reaches 120 ℃, stops to send nitrogen, naturally cooling can be reused.
According to the method described above, this high alpha-olefin polymerization single polymerization monomer refinement treatment device as shown in Figure 1, by Raw material pail 53, feeding pump 52, raw material storage tank 50, molecular sieve adsorption post group, micro-moisture tester 35, tachograph 48, refining raw material storage tank 40 and connect their pipeline, a plurality of valve is formed.Feeding pump 52 is connected with Raw material pail 53 by pipeline, and link to each other with raw material storage tank 50 tops with raw material feed liquor valve 1 by the road, also have nitrogen intake valve 2 and blow-off valve 3 on raw material storage tank 50 tops, its underpart has tap valve 51 and liquid-outlet valve 49 to connect tachograph 48 by the road, feed liquor valve 47 links to each other with molecular sieve adsorption post group lower end, molecular sieve adsorption post group upper end connects micro-moisture tester 35 also by the road through liquid-outlet valve 25 (or 31), feed liquor valve 39 is attached thereto from refining raw material storage tank 40 tops, liquid-outlet valve 41 and tap valve 42 are arranged at refining raw material storage tank 40 bottoms, and its top also has blow-off valve 37 and nitrogen intake valve 38 and tensimeter 36.Molecular sieve adsorption post group wherein can be single-column, twin columns, four posts or six posts, and it is shaped as open tubular column, and its two ends respectively have tubule to communicate, and post is connected with the slow transition of pipe.Concrete constitute be: for single-column is to connect molecular sieve feed liquor valve 47, molecular sieve adsorption post 17, liquid-outlet valve 16,25 after the liquid-outlet valve 49 that picks out from raw material storage tank 50 bottoms and the tachograph 48 to receive micro-moisture tester 35 input terminuss again, and there is tap valve 46 molecular sieve adsorption post 17 lower ends; Bimolecular sieve adsorption column is to tap into liquid valve 47 after tachograph 48, one the tunnel taps into liquid valve 19, molecular sieve adsorption post 17, liquid-outlet valve 16, flow process control valve 15,24 to liquid-outlet valve 25 receives micro-moisture tester 35, another road also connects micro-moisture tester 35 through flow process control valve 45,43, feed liquor valve 20, molecular sieve adsorption post 21, liquid-outlet valve 23 to liquid-outlet valve 25, and is connected between flow process control valve 15 and 24 after having pipeline up to connect flow process control valve 18,22 between the flow process control valve 45 and 43 of bottom; Four molecular sieve adsorption posts are to tap into liquid valve 14, molecular sieve adsorption post 13, liquid-outlet valve 11 and feed liquor valve 26, molecular sieve adsorption post 28, liquid-outlet valve 29 on the twin columns basis on the liquid-outlet valve 16 and 23 of molecular sieve adsorption post 17 and 21 respectively again, after two liquid-outlet valves 11 and 29 upper ends are by 10,30 series connection of flow process control valve, link to each other, connect raw material liquid-outlet valve 31 at valve 30 again with 29 node place and be connected, and connecing handing-over mutually between the flow process control valve 10,30 on flow process control valve 27,12 and top between the flow process control valve 15,24 again with micro-moisture tester 35 input terminuss; Six column molecular sieve adsorption columns are to connect two again on four column foundations molecular sieve adsorption posts and four posts of string mutually also also have identical liquid in-out valve and flow process control valve therebetween mutually up and down.For secluding air condition and the requirement of regenerating molecular sieve flow process, the supporting with it nitrogen device in addition of realizing the molecular sieve treatment process.Nitrogengas cylinder 5 outlet connect tensimeter 7 and nitrogen air outlet valve 6 by the road after, the one tunnel links to each other with raw material storage tank 50 tops through nitrogen intake valve 2, with the processing environment of realization secluding air; Another road heater via intake valve 8 links to each other with nitrogen heater 34, these nitrogen heater 34 outlets link to each other through liquid-outlet valve 16 exit end of nitrogen air outlet valve 33 with unit molecule sieve adsorption column 17, or link to each other with liquid-outlet valve 16,23 exit end of bimolecular sieve adsorption column 17,21, or link to each other with liquid-outlet valve 11,29 exit end of four molecular sieve adsorption posts 17,21,13,28, or link to each other with the exit end of three liquid-outlet valves in six molecular sieve adsorption posts upper ends, the while connects a tap valve respectively again under the feed liquor valve of the nethermost molecular sieve adsorption post of one group of molecular sieve adsorption column.This device has four kinds of array modes with regard to the composition of its molecular sieve adsorption post, but from can continuous production and have enough turnout and quality to weigh, and the structure with four molecular sieve adsorption posts in four kinds of array modes is the best.It is actually two and handles lines, and every line has 2 molecular sieves to go here and there mutually to handle, and can guarantee the quality handled, and the treatment capacity of single-column twice is arranged again.Producing need carry out the manipulation of regeneration flow process after for some time the time simultaneously, can line of manipulation of regeneration, and another line still can continue to produce, and manipulation of regeneration and production are neglected neither, and realizes continuous production.In addition during the manipulation of regeneration flow process, except two molecular sieve adsorption posts of a line of above-mentioned processing, be cross-linked regeneration, the manipulation of regeneration of last two posts or time two posts up and down by what a plurality of flow process control valves of switch also can be realized four posts.Can realize the manipulation of regeneration flow process of the molecular sieve adsorption post of need manipulation of regeneration very neatly.
Embodiment
Embodiment: with four column molecular sieve adsorption column structures is example, sees Fig. 1 for details.Dress potassium A type 3A molecular sieve in each molecular sieve adsorption post 17,21,13 and 28.Column dimension is φ 200 * 1000mm, and valve is selected the Q21F-40P type for use, and micro-moisture tester 35 is selected the MS-2100N type for use, and tachograph 48 is selected the LUGB-22-02E-B type for use, and nitrogen heater 34 is selected the RA-150-4 type for use.Before beginning production, close nitrogen valve 8 earlier, 9 and 32, close the valve 1 of raw material storage tank 50,3,51, the valve 37 of refining raw material storage tank 40,38,41, open nitrogen air outlet valve 6, nitrogen intake valve 2, liquid-outlet valve 49, feed liquor valve 47, flow process control valve 45,43, feed liquor valve 19,20 and valve 16,14,23,26,11,10,30,29,31,25,39, open flow process control valve 18 simultaneously, 22,15,24,27,12,2 atmospheric nitrogen by nitrogen pot 5 blew one minute, with raw material storage tank 50, four molecular sieve adsorption posts 17,21,13,28, after blowing off, air in refining raw material storage tank 40 and all pipelines closes nitrogen air outlet valve 6, nitrogen intake valve 2, while closing flow path control valve 18,22,15,24,27,12,25, other valve such as preceding state, open raw material feed liquor valve 1, open feeding pump 52, liquid starting material is squeezed into raw material storage tank 50, and then open nitrogen air outlet valve 6 and nitrogen intake valve 2, normal temperature nitrogen begins to be pressed into raw material storage tank 50, regulate the size that nitrogen air outlet valve 6 is opened, make the raw material fluid press to four molecular sieve adsorption posts 17 with the speed of 0.05～0.1m/s, 21,13 and 28, stock liquid is from raw material liquid-outlet valve 31, micro-moisture tester 35 enters refining raw material storage tank 40, has finished refinement treatment.When micro-moisture tester 35 shows that moisture soon exceed standard, begin molecular sieve is carried out the manipulation of regeneration flow process respectively, as at first right side two molecular sieve adsorption posts 21,28 being carried out manipulation of regeneration, and left side two molecular sieves 17,13 are still being produced.At this moment as long as closing flow path control valve 45,43,18,22,15,24,27,12,10,30, open nitrogen heater intake valve 8, nitrogen air outlet valve 33, nitrogen intake valve 32, tap valve 44, the Heating temperature of regulating nitrogen heater 34 makes nitrogen temperature reach 380 ℃, detection molecules is sieved the temperature in adsorption column 21 exits simultaneously, after reaching 120 ℃, kept 2.5 hours, close well heater intake valve 8, nitrogen air outlet valve 33, nitrogen intake valve 32 and tap valve 44, treat to put into production again behind the naturally cooling.The manipulation of regeneration of left side two molecular sieve adsorption posts 17,13 is also similar.This device can be realized single-column, single-column series connection, twin columns parallel connection and four kinds of technical process of twin columns series connection, and can carry out regenerating molecular sieve to single-column, twin columns even three posts, four posts and handle by each flow process control valve of control, uses flexibly, and is easy to operate.Through the high alpha-olefin polymerization single polymerization monomer of this device and present method processing, its contained humidity can be removed to low-down level, reaches＜1ppm.To the molecular sieve check, its adsorbable material mass can reach 20% of molecular sieve quality, and adsorbable other material except that moisture, as oxygen, carbon monoxide, carbonic acid gas and low-molecular olefine etc.
As from the foregoing, the present invention's method is easy, and device is simple, and operating procedure is flexible, the object of molecular sieve adsorption is many, adsorptive capacity is big, and the quality of dehydration and other impurity is good, the efficient height, adsorbable material can reach more than 20% of molecular sieve quality, and the use of molecular sieve iterative regenerable, and manipulation of regeneration is simple, thereby reduce the refinement treatment cost of high alpha-olefin polymerization single polymerization monomer greatly.
Description of drawings
The high alpha-olefin polymerization single polymerization monomer refinement treatment setting drawing of Fig. 1 four molecular sieve adsorption posts
Wherein
1-raw material feed liquor valve, 2-nitrogen intake valve
3-blow-off valve, 4-tensimeter
5-nitrogengas cylinder, 6-nitrogen air outlet valve
7-tensimeter, 8-well heater intake valve
9-nitrogen intake valve, 10-flow process control valve
11-liquid-outlet valve, 12-flow process control valve
13-molecular sieve adsorption post, 14-feed liquor valve
15-flow process control valve, 16-liquid-outlet valve
17-molecular sieve adsorption post, 18-flow process control valve
19-feed liquor valve, 20-feed liquor valve
21-molecular sieve adsorption post, 22-flow process control valve
23-liquid-outlet valve, 24-flow process control valve
25-liquid-outlet valve, 26-feed liquor valve
27-flow process control valve, 28-molecular sieve adsorption post
29-liquid-outlet valve, 30-flow process control valve
31-liquid-outlet valve, 32-nitrogen intake valve
33-nitrogen air outlet valve, 34-nitrogen heater
35-micro-moisture tester, 36-tensimeter
37-blow-off valve, 38-nitrogen intake valve
39-feed liquor valve 40-refining raw material storage tank
41-liquid-outlet valve, 42-tap valve
43-flow process control valve, 44-tap valve
45-flow process control valve, 46-tap valve
47-feed liquor valve, 48-tachograph
49-liquid-outlet valve, 50-raw material storage tank
51-tap valve, 52-feeding pump
53-Raw material pail
Claims (8)
1. high alpha-olefin polymerization single polymerization monomer fine purification treatment process is stored in refining raw material storage tank after it is characterized in that in the environment of secluding air the high alpha-olefin polymerization single polymerization monomer solution from bottom to top sent into one group of molecular sieve adsorption column from raw material storage tank.
2. a kind of high alpha-olefin polymerization single polymerization monomer fine purification treatment process according to claim 1, it is characterized in that with nitrogen with raw material storage tank, molecular sieve adsorption post group, refining raw material storage tank and after connecting air in their pipeline and blowing off, the high alpha-olefin polymerization single polymerization monomer solution that will inject raw material storage tank with normal temperature nitrogen is from bottom to top pressed with the flow velocity of 0.05～0.1m/s and is sent into refining raw material storage tank through one group of molecular sieve adsorption column and through after the assay was approved.
3. according to claim 1,2 described a kind of high alpha-olefin polymerization single polymerization monomer fine purification treatment process, it is characterized in that it can be single-column or twin columns (parallel connection) or twin columns (parallel connection) series connection or three posts (parallel connection) series connection that described molecular sieve adsorption post is looked the size of treatment capacity.
4. according to claim 1,2 described a kind of high alpha-olefin polymerization single polymerization monomer fine purification treatment process, it is characterized in that described molecular sieve is best with potassium A type 3A molecular sieve, its chemical ingredients is 0.66K
2O034Na
2OAl
2O
32.0SiO
24.5H
2O.
5. according to claim 1,2 described a kind of high alpha-olefin polymerization single polymerization monomer fine purification treatment process, it is characterized in that the molecular sieve adsorption post has the regenerating molecular sieve treatment scheme, when recording Moisture high UCL by online micro-moisture tester, stop liquor charging, normal temperature nitrogen directly is pressed into each molecular sieve adsorption post expel liquid with 2 atmospheric pressure, after be that 2 atmospheric nitrogen are sent into the molecular sieve adsorption post again with 350～400 ℃ of pressure, after reaching 120 ℃, molecular sieve adsorption column outlet nitrogen temperature kept 2～3 hours, stop to send nitrogen, naturally cooling can be reused.
6. high alpha-olefin polymerization single polymerization monomer refinement treatment device, it is characterized in that this device is by Raw material pail [53], feeding pump [52], raw material storage tank [50], molecular sieve adsorption post group, micro-moisture tester [35], tachograph [48], refining raw material storage tank [40] and connect their pipeline, a plurality of valves are formed, feeding pump [52] is connected with Raw material pail [53] by pipeline, and link to each other with raw material storage tank [50] top with raw material feed liquor valve [1] by the road, also have nitrogen intake valve [2] and blow-off valve [3] on raw material storage tank [50] top, its underpart has liquid-outlet valve [49] to connect tachograph [48] by the road, feed liquor valve [47] links to each other with molecular sieve adsorption post group lower end, and the upper end of molecular sieve adsorption post group connects micro-moisture tester [35] also by the road through material outlet valve [25] (or [31]), inlet valve [39] is attached thereto from refining raw material storage tank [40] top.
7. a kind of high alpha-olefin polymerization single polymerization monomer refinement treatment device according to claim 6, the molecular sieve adsorption post group that it is characterized in that being contained between raw material storage tank [50] and the refining raw material storage tank [40] can be single-column, twin columns, four posts or six posts, single-column is that the liquid-outlet valve [49] and the tachograph [48] that pick out from raw material storage tank [50] bottom tap into liquid valve [47], molecular sieve adsorption post [17], liquid-outlet valve [16], [25] afterwards, receive micro-moisture tester [35] input terminus again, and molecular sieve adsorption post [17] lower end there is tap valve [46]; Twin columns are to tap into liquid valve [47] afterwards at tachograph [48], one the tunnel taps into liquid valve [19], molecular sieve adsorption post [17], liquid-outlet valve [16], flow process control valve [15], [24] to liquid-outlet valve [25] receives micro-moisture tester [35], another road also connects micro-moisture tester [35] through flow process control valve [45], [43], feed liquor valve [20], molecular sieve adsorption post [21], liquid-outlet valve [23] to liquid-outlet valve [25], and is connected between flow process control valve [15], [24] after having pipeline up to connect flow process control valve [18], [22] between the flow process control valve [45] of bottom and [43]; Four posts are to tap into liquid valve [14] respectively again on the twin columns basis on the liquid-outlet valve [16] of molecular sieve adsorption post [17] and [21] and [23], molecular sieve adsorption post [13], liquid-outlet valve [11] and feed liquor valve [26], molecular sieve adsorption post [28], liquid-outlet valve [29], in two liquid-outlet valves [11] and [29] upper end by flow process control valve [10], [30] the series connection back links to each other, connect raw material liquid-outlet valve [31] at the node place of valve [30] and [29] again and join with micro-moisture tester [35] input terminus, and in flow process control valve [15], [24] connect flow process control valve [27] between again, [12] with the flow process control valve [10] on top, [30] be connected between; Six posts are to connect 2 again on above-mentioned four column foundations molecular sieve adsorption posts and four posts of string mutually also also have identical liquid inlet and outlet valve and flow process control valve therebetween mutually up and down.
8. according to claim 6,7 described a kind of high alpha-olefin polymerization single polymerization monomer refinement treatment devices, [5] outlet that it is characterized in that nitrogengas cylinder is arranged connect tensimeter [7] and nitrogen air outlet valve [6] by the road one road heater via intake valve [8] link to each other with nitrogen heater [34], this well heater [34] outlet links to each other through liquid-outlet valve [16] exit end of nitrogen air outlet valve [33] with unit molecule sieve adsorption column [17], or with bimolecular sieve adsorption column [17], [21] liquid-outlet valve [16], [23] exit end links to each other, or with four molecular sieve adsorption posts [17], [21], [13], [28] liquid-outlet valve [11], [29] exit end links to each other, or link to each other with the exit end of three liquid-outlet valves in upper end of six molecular sieve adsorption posts, under the feed liquor valve of the nethermost molecular sieve adsorption post of one group of molecular sieve adsorption column, respectively be connected to a tap valve simultaneously; Another road links to each other with raw material storage tank [50] top through nitrogen intake valve [2].
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102952047A (en) * | 2011-08-30 | 2013-03-06 | 中国石油化工股份有限公司 | 2-acrylamide-2-methylpropanesulfonic acid (AMPS) crude product and refining method thereof |
| CN102952045A (en) * | 2011-08-30 | 2013-03-06 | 中国石油化工股份有限公司 | 2-acrylamide-2-methylpropanesulfonic acid (AMPS) crude product and refining method thereof |
| CN102952046A (en) * | 2011-08-30 | 2013-03-06 | 中国石油化工股份有限公司 | 2-acrylamide-2-methylpropanesulfonic acid (AMPS) crude product and refining method thereof |
| CN105062555A (en) * | 2015-07-23 | 2015-11-18 | 中国科学院上海高等研究院 | Method for synthesizing metallocene poly-alpha-olefin from alpha-olefin-prepared-from-coal as raw material |
| CN105272809A (en) * | 2014-07-17 | 2016-01-27 | 中国科学院上海高等研究院 | Removal method of oxygen-containing compounds in coal alpha-olefins |
| CN112129018A (en) * | 2020-10-19 | 2020-12-25 | 中国科学院理化技术研究所 | Combined cold accumulator and liquid air energy storage system |
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2003
- 2003-09-27 CN CNB031348823A patent/CN100513366C/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102952047A (en) * | 2011-08-30 | 2013-03-06 | 中国石油化工股份有限公司 | 2-acrylamide-2-methylpropanesulfonic acid (AMPS) crude product and refining method thereof |
| CN102952045A (en) * | 2011-08-30 | 2013-03-06 | 中国石油化工股份有限公司 | 2-acrylamide-2-methylpropanesulfonic acid (AMPS) crude product and refining method thereof |
| CN102952046A (en) * | 2011-08-30 | 2013-03-06 | 中国石油化工股份有限公司 | 2-acrylamide-2-methylpropanesulfonic acid (AMPS) crude product and refining method thereof |
| CN105272809A (en) * | 2014-07-17 | 2016-01-27 | 中国科学院上海高等研究院 | Removal method of oxygen-containing compounds in coal alpha-olefins |
| CN105272809B (en) * | 2014-07-17 | 2017-04-26 | 中国科学院上海高等研究院 | Removal method of oxygen-containing compounds in coal alpha-olefins |
| CN105062555A (en) * | 2015-07-23 | 2015-11-18 | 中国科学院上海高等研究院 | Method for synthesizing metallocene poly-alpha-olefin from alpha-olefin-prepared-from-coal as raw material |
| CN105062555B (en) * | 2015-07-23 | 2018-04-24 | 中国科学院上海高等研究院 | A kind of coal alpha-olefin is the method for Material synthesis metallocene poly alpha olefin |
| CN112129018A (en) * | 2020-10-19 | 2020-12-25 | 中国科学院理化技术研究所 | Combined cold accumulator and liquid air energy storage system |
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| CN100513366C (en) | 2009-07-15 |
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