CN101591215A - The water-retaining agent that uses in a kind of normal-temperature propylene refining technology and this technology - Google Patents
The water-retaining agent that uses in a kind of normal-temperature propylene refining technology and this technology Download PDFInfo
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Abstract
The present invention relates to a kind of water-retaining agent that can be used for the propylene feedstocks process for refining, described water-retaining agent is one or more in crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, sex change PVA, polyacrylamide, starch grafted acrylate, starch and acrylic acid acrylamide and the tetrapolymer that forms along acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification hydrolyzate, the distortion polyvinyl alcohol, or one or more the mixture in one or more and solid alkali in the above-mentioned substance, A type molecular sieve, the aluminum oxide.The present invention is also disclosing on the basis of above-mentioned water-retaining agent, the water-retaining agent that uses above-mentioned high dehydration capacity and the propylene feedstocks process for refining of high Sulfur capacity sweetening agent are further disclosed, this technology has improved the propylene refining ability on the whole, more can satisfy the demand of propylene refining device long period, heavy-duty service, purification efficiency is very high.
Description
Technical field
The present invention relates to a kind of water-retaining agent and use the normal-temperature propylene refining technology of this water-retaining agent, belong to the propylene refining technical field.
Background technology
The polypropylene synthesis technique is to be raw material with the propylene, under catalyst action, generates organic high molecular polymer through polyreaction.In the polypropylene synthesis technique, except that the perfect of process for refining itself with effectively controlling, quality control to propylene feedstocks also is vital, because if the detrimental impurity content height in the propylene feedstocks, will influence activity of such catalysts and orientation property, even cause poisoning of catalyst that polyreaction can not be taken place, and then influence quality product.
Liquid propylene process for refining route at present commonly used mainly comprises three kinds:
First operational path is the dehydration of (1) free-water knockout, (2) COS hydrolytic reagent and sweetening agent desulfurization, (3) 3A molecular sieve dehydration, (4) rectifying tower removal O
2, H
2, CO, CO
2Deng hydrocarbon component, (5) 3A molecular sieve dehydration;
Second operational path is that (1) solid alkali NaOH dehydration, (2) 3A molecular sieve dehydration, (3) COS hydrolytic reagent and sweetening agent desulfurization, (4) rectifying tower are removed O
2, H
2, CO, CO
2Deng hydrocarbon component, (5) 3A molecular sieve dehydration;
The 3rd operational path is that (1) 3A molecular sieve dehydration, (2) C18 type catalyzer take off CO, the deoxidation of (3) BH type catalyzer, (4) COS hydrolytic reagent and sweetening agent desulfurization, (5) 3A molecular sieve dehydration.
As mentioned above, the detrimental impurity in the propylene feedstocks comprises water, sulfide, CO and oxygen etc.Take off CO and dearsenification for propylene feedstocks is refining, the carbon monoxide that commonly used in the market is in the C18 catalyst removal propylene, the C18 catalyzer will be regenerated in the nitrogen of certain flow in use for some time.Dearsenic agent commonly used is CuO/r-Al
2O
3, PbO/r-Al
2O
3, after dearsenic agent adsorbs a certain amount of arsenic, the dearsenification ability drop, arsenic content improves in the propylene, will note changing dearsenic agent this moment.Present removal of carbon monoxide in the propylene feedstocks process for refining and dearsenic technique comparative maturity all.
Relevant propylene feedstocks is made with extra care deoxidation, and reductor commonly used comprises two types, and a kind of is BH type reductor (nickel catalyst), and another kind is a manganese series catalyzer.Because BH type reductor cost height, so the propylene feedstocks process for refining is selected manganese deoxidier (is active ingredient with MnO, MnO+FeO etc.) mostly, such reductor cost is low, and is active high.Disclose a kind of manganese deoxidier such as Chinese patent literature CN200510116710.1, this reductor is with MnO/Mn
3O
4Be active constituent, add accelerative activator alkaline earth metal oxide and aluminum oxide; The reductor of this invention can remove the oxygen of 1～2000ppm in ethene, the propylene etc., has the higher deoxidation degree of depth, deoxidation capacity and activity.In addition, Chinese patent literature CN200610113865.4 then discloses a kind of Mn-Ag dual-active component reductor, and reductor is with Mn
3O
4Be main active component, contained therein a small amount of Ag
2Under the katalysis of O, reduce Mn significantly
3O
4Be reduced into the temperature and time of the low price MnO with deoxy activity; The reductor of this invention can be at 80～160 ℃ of reducing/regeneratings, under the room temperature micro amount of oxygen in ethene, the propylene etc. is purified to 0.05ppm, the reductor of this invention is used for polyolefin industry and produces, can prolong the reductor regeneration period, avoid polymerizing catalyst to poison, reduce production costs, have tangible economic benefit.
For crude propylene, because wherein the content of water and sulfide is bigger, so propylene feedstocks purified emphasis is dehydration and desulfurization.Water in the propylene feedstocks can with catalyzer and activator generation vigorous reaction, thereby make catalyst activity reduction; When water-content is higher than 100ug/g, propylene polymerization can not take place; Sulphur in the propylene feedstocks can make the polyreaction chain termination on the one hand, can make catalyst activity reduction on the other hand, thereby causes the plasticizing piece occurring even stopping up still in the decline of polyolefine output, degree of isotacticity decline, the powder, influences production process and production efficiency.
In the prior art, under the condition of normal temperature, certain pressure, dehydration technique commonly used mainly is to adopt solid alkali, aluminum oxide or molecular sieve as water-retaining agent in the propylene refining technology.Wherein, select to use propylene refining solid caustic soda tower that propylene feedstocks is dewatered, owing to also have the part acidic components in the propylene feedstocks, so cause a solid alkali part and above-mentioned acidic components to react, another part solid alkali just can really play the effect of water-retaining agent; Using this part solid alkali to carry out in the dehydration, because moisture is bigger in the propylene feedstocks system, and mostly be free-water, this portion water can't all be condensed the back and normally be removed by return tank, this part free-water meeting and this part solid alkali effect that can't normally remove so, thereby make the solid caustic soda tower ineffective, and very easily stop up and cut the liquid caustic soda line.Time long back liquid caustic soda liquid level superelevation is flooded opening for feed, and propylene feedstocks can at first be passed the liquid caustic soda layer in the solid caustic soda tower so, the portable propylene of bringing into of sulfur-containing impurities wherein, and cause alkali lye to be carried into the molecular sieve tower easily, and cause the molecular sieve tower to lose efficacy, can't dewater.In addition, if use aluminum oxide or molecular sieve to dewater, because the dehydration finite capacity of aluminum oxide and molecular sieve, activated alumina Static Water adsorption range is generally at 150-170mg/g, the scope of molecular sieve Static Water absorption is generally between 200-265mg/g, so it is easy to reach capacity, so need often switch drying chamber, discharging propylene, nitrogen replacement, the operating process of nitrogen temperature regenerated, thereby cause propylene discharging torch pipe network amount to increase, recirculated water, nitrogen, electricity etc. consumptions increase, and are to have increased the device operation cost even more importantly.Similarly, the solid caustic soda water-intake rate can not reach 15% of own wt, but also is easy to deliquescence, so the technical problem that the problems referred to above existed when also being to use solid alkali.
Sulphur in the propylene is mainly based on organosulfur (carbonylsulfide COS), to removing of this partial vulcanization thing, at first need be under the hydrolytic reagent effect organosulfur be converted into inorganic sulfur (H
2S), use sweetening agent that inorganic sulfur is removed then.Show after deliberation, sweetening agent commonly used all has certain Sulfur capacity, and for the propylene refining desulfurization, when the sulfur capacity of sweetening agent reaches 2% (massfraction) left and right sides, the sweetening effectiveness of sweetening agent just begins to occur downtrending, and just should in time change sweetening agent this moment.Propylene feedstocks sweetening agent commonly used at present comprises that with zinc oxide or cupric oxide be the sweetening agent of active ingredient; A kind of gaseous state of sulfur-bearing, ambient temperature desulfuration agent of liquid material of can be used for disclosed such as Chinese patent literature CN1094331, this sweetening agent is made up of main raw material ZnO and structural promoter iron cement, shows that after tested the actual Sulfur capacity that this sweetening agent uses at normal temperatures can only reach about 5%.Chinese patent literature CN00114588.6 discloses a kind of sweetening agent that can be used for the fine desulfurizing technology of production technique such as synthetic polypropylene, and this sweetening agent is made up of the oxide compound of Na, Cu, Si or salt and gac; This sweetening agent can remove H simultaneously
2S, COS, CS
2, mercaptan, thioether, thiophene sulfides, be particularly useful for smart mercaptan removal, thioether, it removes precision＜0.05ppm.In a word, the Sulfur capacity of propylene refining sweetening agent commonly used is all very low in the prior art.For propylene refining technology, the propylene unit volume space velocity increases or sulphur content increases, and will cause the time length of desulfurization to shorten, so that need the frequent sweetening agent of changing, has increased operation cost, has reduced production efficiency.Therefore in the propylene feedstocks process for refining, need the high sweetening agent of Sulfur capacity.
Summary of the invention
It is the low problem of water-retaining agent dehydration capacity in the propylene feedstocks process for refining in the prior art that the present invention will solve first technical problem, and then provides a kind of and have high dehydration capacity, do not need it is carried out the water-retaining agent that frequent constantly regenerated can be used for propylene refining.
It is that the sweetening agent Sulfur capacity is lower in of the prior art third rare process for refining that the present invention will solve second technical problem, need constantly to regenerate and change sweetening agent, cause the low problem of purification efficiency, and then provide a kind of and use high dehydration capacity water-retaining agent and have the sweetening agent of high Sulfur capacity and have the propylene refining novel process of high purification efficiency water-retaining agent.
For solving the problems of the technologies described above, the invention provides a kind of water-retaining agent that can be used for the propylene feedstocks process for refining, described water-retaining agent is a crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, modified polyvinyl alcohol PVA, polyacrylamide, starch grafted acrylate, starch and acrylic acid acrylamide and the tetrapolymer that forms along acid anhydrides, the cellulose graft acrylate, starch-grafted vinyl cyanide saponification hydrolyzate, distortion one or more in polyvinyl alcohol, or one or more and solid alkali in the above-mentioned substance, A type molecular sieve, the mixture of one or more in the aluminum oxide.
The present invention is also disclosing on the basis of above-mentioned water-retaining agent, further discloses a kind of propylene feedstocks process for refining that uses above-mentioned water-retaining agent, and it comprises the steps:
(a) in dehydration reactor, fill water-retaining agent, described water-retaining agent be crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, sex change PVA, polyacrylamide, starch grafted acrylate, starch, acrylic acid acrylamide, along in acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification hydrolyzate, the distortion polyvinyl alcohol one or more, or one or more the mixture in one or more and solid alkali in the above-mentioned substance, A type molecular sieve, the aluminum oxide; Propylene feedstocks is by filling the dehydration reactor of described water-retaining agent, is that 10 ℃～40 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by the water-retaining agent bed is 0.5～5.0h in temperature of reaction
-1Condition under, propylene feedstocks is carried out processed;
(b) propylene after dehydration enter be filled with take off the CO catalyzer take off the CO reactor, be that 10 ℃～50 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by taking off CO catalyzer agent bed is 0.5～5.0h in temperature of reaction
-1Condition under, propylene feedstocks is taken off CO handles;
(c) propylene after taking off CO and handling enters the deoxidation reactor that is filled with nickel deoxidier or manganese deoxidier, is 10 ℃～50 ℃ in temperature of reaction, and pressure is 1.0MPa～5.0Mpa, and the volume space velocity by dehydrogenation catalyst agent bed is 0.5～5.0h
-1Condition under, propylene feedstocks is carried out deoxidation treatment;
(d) propylene after deoxidation treatment enters cos hydrolysis reactor that is filled with hydrolytic catalyst of carbonyl sulfur respectively and the desulphurization reactor that is filled with sweetening agent successively, described sweetening agent is a FeOOH desulfurizer, and this sweetening agent comprises the hydrous iron oxide of 30～60wt%; In temperature of reaction is that 10 ℃～50 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by hydrolytic catalyst of carbonyl sulfur and FeOOH desulfurizer bed is 0.5～10h
-1Condition under, propylene feedstocks is carried out desulfurization handles.
In aforesaid propylene feed purification technology, preferably after described step (d) propylene feedstocks being entered the dehydration reactor that is filled with the 3A molecular sieve, is that 10 ℃～50 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by the dewatering agent bed is 0.5～5h in temperature of reaction
-1Condition under, propylene feedstocks is carried out deep dehydration.
In aforesaid propylene feed purification technology, the described CO of taking off catalyzer is the C18 catalyzer.Described hydrolytic catalyst of carbonyl sulfur is by active ingredient Cs
2O, K
2O, Na
2O, CaO, ZnO, BaO, MgO, Fe
2O
3In one or more, r-Al
2O
3Carrier or TiO
2The r-Al of modification
2O
3Complex carrier is formed; Described active component content is 1～40wt% of total catalyst weight.
Wherein, described FeOOH desulfurizer obtains as follows:
(e), be to mix in 1: 2～1: 3 by iron and mol ratio hydroxy with solid ferrous compound and solid hydroxide;
(f) step (e) gained mixture is finished reaction by mixing to pinch, in described kneading process, the control temperature of charge is no more than 70 ℃;
(g) step (f) gained reaction product is dried in air;
(h) to washing of step (g) gained material and filtration;
(i) with step (h) gained solid seasoning or in 70 ℃～90 ℃ oven dry.
The present invention has advantage as described below:
(1) in the propylene feedstocks process for refining of the present invention, adopted polymer water-absorbent crosslinked salt polyacrylate with super-strong moisture absorbing performance, vinyl alcohol-acrylate segmented copolymer, sex change PVA, polyacrylamide, starch grafted acrylate, starch, acrylic acid acrylamide, along in acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification hydrolyzate, the distortion polyvinyl alcohol one or more, or one or more the mixture in one or more and solid alkali in the above-mentioned substance, A type molecular sieve, the aluminum oxide; This water-retaining agent has bigger water adsorption capacity, the state of saturation that arrives its absorption free-water can satisfy a plurality of propylene refining cycles and use, so it does not need often to switch drying chamber, discharging propylene, nitrogen replacement, water-retaining agent is carried out the operating process of nitrogen temperature regenerated, reduce process for refining running cost on the whole, improved purification efficiency;
(2) use FeOOH desulfurizer to remove sulfide in the propylene in the propylene feedstocks process for refining of the present invention, this sweetening agent can be realized scale operation, its cost is low, and has higher Sulfur capacity, shows that after tested the Sulfur capacity of this sweetening agent can be up to 52%; This Sulfur capacity can guarantee to improve the replacement cycle of sweetening agent, thereby has reduced the running cost of process for refining;
(3) water-retaining agent with high dehydration capacity and sweetening agent have been used in the propylene feedstocks process for refining of the present invention with high Sulfur capacity, acting in conjunction by said two devices, improved the propylene refining ability on the whole, more can satisfy propylene refining device long period, heavy-duty service, processing by this technology can be brought up to the high-quality level with the quality of propylene feedstocks, and purification efficiency is very high.
Embodiment
Employed FeOOH desulfurizer is special in the propylene feedstocks process for refining of the present invention, and following embodiment 1～9 has carried out describing further to its preparation:
Embodiment 1
32g ferrous sulfate powder and 12g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.8; The said mixture material is put into kneader, pinch 3h and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards, be beneficial to fully finishing of above-mentioned reaction thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is dried, and bake out temperature is 80 ℃, and drying time is 3h, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 2
64g ferrous sulfate powder and 21.2g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.4; The said mixture material is put into kneader, pinch 0.5h and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is carried out seasoning, and drying temperature is-5 ℃, and be 10h time of drying, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 3
34.2g Iron nitrate powder and 23.4g potassium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.0; The said mixture material is put into kneader, pinch 1.0h and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is carried out seasoning, and drying temperature is 45 ℃, and drying time is 3h, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 4
64g ferrous sulfate powder and 22g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.5; The said mixture material is put into kneader, pinch 15min and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is dried, and bake out temperature is 90 ℃, and drying time is 3h, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 5
64g ferrous sulfate powder and 22g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.5; The said mixture material is put into kneader, pinch 2.0h and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is carried out seasoning, and drying temperature is 30 ℃, and be 1h time of drying, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 6
64g ferrous sulfate powder and 22g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.5; The said mixture material is put into kneader, pinch 25min and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is carried out seasoning, and drying temperature is 30 ℃, and be 1h time of drying, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 7
64g ferrous sulfate powder and 20g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.3; The said mixture material is put into kneader, pinch 30min and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is dried, and bake out temperature is 100 ℃, and drying time is 1h, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 8
92g ferrous sulfate powder and 28g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 2.2; The said mixture material is put into kneader, pinch 30min and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is carried out seasoning, and drying temperature is 45 ℃, and be 1h time of drying, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
Embodiment 9
20.9g iron protochloride powder and 21.7g sodium hydroxide are mixed, and wherein, iron and mol ratio hydroxy are 1: 3.0; The said mixture material is put into kneader, pinch 30min and finish solid state reaction between the above-mentioned reactant, above-mentioned reaction product is placed in the air dries afterwards thereby mix.
Material after will drying adds water earlier and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (checking with bariumchloride usually).
Above-mentioned solid behind washing and filtering is carried out seasoning, and drying temperature is 45 ℃, and be 1h time of drying, can make amorphous FeOOH desulfurizer required in the propylene refining technology of the present invention.
In the foregoing description 1～9, employed ferrous sulfate powder is FeSO
47H
2O content is the industrial raw material of 88～90wt%; In the sodium hydroxide in the content of NaOH or the potassium hydroxide content of KOH be 90～93wt%; Baking step carries out in electric drying oven with forced convection; The model of employed kneader is the polyfunctional catalyst shaper of CD4 * 1TS, and certainly, any commercially available kneader that can realize the object of the invention all goes for the present invention.
Embodiment 10
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: 1. select the 20g crosslinked salt polyacrylate as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O and carrier r-Al
2O
3Form, wherein active component content is the 1wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 30wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed.Behind above-mentioned process for refining in the propylene water-content less than 1.1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 11
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: 1. select the 20g crosslinked salt polyacrylate as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O and carrier r-Al
2O
3Form, wherein active component content is the 5wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 40wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by deep dehydration agent bed is 2.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 12
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: 1. select the 30g polyacrylamide as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 10 ℃, pressure is 1.0Mpa, and the air speed by the dewatering agent bed is 0.5h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 10 ℃, and pressure is 1.0Mpa, is 0.5h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 10 ℃ that pressure is 1.0Mpa, the air speed by the dehydrogenation catalyst bed is 0.5h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O and TiO
2The r-Al of modification
2O
3Complex carrier is formed, wherein active component content is the 10wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 10 ℃, pressure is 1.0Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 0.5h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 50wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 10 ℃, and pressure is 1.0Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 0.5h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 10 ℃, and pressure is 1.0Mpa, and the air speed by deep dehydration agent bed is 0.5h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 13
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: 1. select the 20g starch grafted acrylate as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O, Fe
2O
3With carrier r-Al
2O
3Form, wherein active component content is the 15wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 60wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by deep dehydration agent bed is 2.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 14
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: 1. select 20g distortion polyvinyl alcohol A as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O, BaO and TiO
2The r-Al of modification
2O
3The composition of complex carrier, wherein active component content is the 20wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 70wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by deep dehydration agent bed is 2.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 15
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: 1. select 30g cellulose graft acrylate as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 50 ℃, pressure is 5.0Mpa, and the air speed by the dewatering agent bed is 5.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 50 ℃, and pressure is 5.0Mpa, is 5.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. taking by weighing the 30g active ingredient is the nickel deoxidier of NiO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 50 ℃ that pressure is 5.0Mpa, and the air speed by the dehydrogenation catalyst bed is 5.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by ZnO, MgO and carrier r-Al
2O
3Form, wherein active component content is the 25wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 50 ℃, pressure is 5.0Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 10.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 80wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 50 ℃, and pressure is 5.0Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 10.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 50 ℃, and pressure is 5.0Mpa, and the air speed by deep dehydration agent bed is 5.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 16
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: 1. select the starch-grafted vinyl cyanide saponification of 20g hydrolyzate as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O, MgO and TiO
2The r-Al of modification
2O
3Complex carrier is formed, wherein active component content is the 30wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 80wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by deep dehydration agent bed is 2.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 17
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: the mixture of 1. selecting 20g starch grafted acrylate and solid alkali is as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by MgO, BaO and carrier r-Al
2O
3Form, wherein active component content is the 35wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 85wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by deep dehydration agent bed is 2.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 18
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: the mixture of 1. selecting 20g sex change PVA and aluminum oxide is as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by CaO, Cs
2O and r-Al
2O
3Form, wherein active component content is the 40wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 90wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by deep dehydration agent bed is 2.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
Embodiment 19
Use in the present embodiment and contain 800ul/L H
2O, 20ul/L CO, 15ul/L O
2, 10ug/g carbonylsulfide sulphur, 5ug/g hydrogen sulfide propylene, treatment step comprises: the mixture of 1. selecting 20g polyacrylamide and solid alkali is as dewatering agent, and it is packed in the dehydration reactor, the temperature of reaction of setting in the reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dewatering agent bed is 3.0h
-1, propylene feedstocks is carried out processed; 2. take by weighing 30g C18 and take off the CO catalyzer, and it is packed into take off in the CO reactor, the temperature of reaction of setting reactor is 30 ℃, and pressure is 1.3Mpa, is 2.0h by the air speed of taking off the CO beds
-1, propylene feedstocks is taken off CO handles; 3. take by weighing the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in the deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃ that pressure is 1.3Mpa, the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take by weighing the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by Na
2O and carrier r-Al
2O
3Form, wherein active component content is the 35wt% of this hydrolyst gross weight, this hydrolyst is packed in the cos hydrolysis reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the hydrolytic catalyst of carbonyl sulfur bed is 2.0h
-1, the carbonylsulfide in the propylene feedstocks is hydrolyzed; 5. take by weighing 30g hydroxyl oxidize iron level and be the sweetening agent of 90wt% and it is packed in the desulphurization reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by the hydrogen sulfide desulphurization agent bed is 2.0h
-1, the hydrogen sulfide in the propylene feedstocks is removed; 6. take by weighing 30g water-retaining agent 3A molecular sieve, and it is packed in the deep dehydration reactor, the temperature of reaction of setting this reactor is 30 ℃, and pressure is 1.3Mpa, and the air speed by deep dehydration agent bed is 2.0h
-1, propylene feedstocks is carried out deep dehydration; Take off the back propylene in water-content less than 1ul/L, CO content less than 0.03ul/L, oxygen level less than 1ul/L, hydrogen sulfide sulphur 0ug/g, carbonylsulfide sulphur less than 0.05ug/g, total sulfur less than 0.5ug/g.
The water-retaining agent of in the foregoing description, mentioning, described water-retaining agent is one or more among crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, modified polyvinyl alcohol PVA, polyacrylamide, starch grafted acrylate, starch and acrylic acid acrylamide and the tetrapolymer that forms along acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification hydrolyzate, the distortion polyvinyl alcohol A, or one or more the mixture in one or more and solid alkali in the above-mentioned substance, A type molecular sieve, the aluminum oxide; Arbitrary combination between the above-mentioned substance all is applicable to the present invention.
Though the present invention elaborates it by above-mentioned specific embodiment; but; the any form that does not exceed the claim protection domain that those skilled in the art should be understood that on this basis to be made and the variation of details all belong to invention which is intended to be protected.
Claims (6)
1. water-retaining agent that can be used for the propylene feedstocks process for refining, it is characterized in that, described water-retaining agent is one or more in crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, modified polyvinyl alcohol PVA, polyacrylamide, starch grafted acrylate, starch and acrylic acid acrylamide and the tetrapolymer that forms along acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification hydrolyzate, the distortion polyvinyl alcohol, or one or more the mixture in one or more and solid alkali in the above-mentioned substance, A type molecular sieve, the aluminum oxide.
2. propylene feedstocks process for refining, it comprises the steps:
(a) in dehydration reactor, fill water-retaining agent, described water-retaining agent be crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, sex change PVA, polyacrylamide, starch grafted acrylate, starch, acrylic acid acrylamide, along in acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification hydrolyzate, the distortion polyvinyl alcohol one or more, or one or more the mixture in one or more and solid alkali in the above-mentioned substance, A type molecular sieve, the aluminum oxide; Propylene feedstocks is by filling the dehydration reactor of described water-retaining agent, is that 10 ℃～40 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by the water-retaining agent bed is 0.5～5.0h in temperature of reaction
-1Condition under, propylene feedstocks is carried out processed;
(b) propylene after dehydration enter be filled with take off the CO catalyzer take off the CO reactor, be that 10 ℃～50 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by taking off CO catalyzer agent bed is 0.5～5.0h in temperature of reaction
-1Condition under, propylene feedstocks is taken off CO handles;
(c) propylene after taking off CO and handling enters the deoxidation reactor that is filled with nickel deoxidier or manganese deoxidier, is 10 ℃～50 ℃ in temperature of reaction, and pressure is 1.0MPa～5.0Mpa, and the volume space velocity by the dehydrogenation catalyst bed is 0.5～5.0h
-1Condition under, propylene feedstocks is carried out deoxidation treatment;
(d) propylene after deoxidation treatment enters cos hydrolysis reactor that is filled with hydrolytic catalyst of carbonyl sulfur and the desulphurization reactor that is filled with sweetening agent successively, described sweetening agent is a FeOOH desulfurizer, and this sweetening agent comprises the hydrous iron oxide of 30～90wt%; In temperature of reaction is that 10 ℃～50 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by hydrolytic catalyst of carbonyl sulfur and FeOOH desulfurizer bed is 0.5～10h
-1Condition under, propylene feedstocks is carried out desulfurization handles.
3. propylene feedstocks process for refining according to claim 2, it is characterized in that, after described step (d) propylene feedstocks being entered the dehydration reactor that is filled with the 3A molecular sieve, is that 10 ℃～50 ℃, pressure are 1.0MPa～5.0Mpa, volume space velocity by the dewatering agent bed is 0.5～5h in temperature of reaction
-1Condition under, propylene feedstocks is carried out deep dehydration.
4. propylene feedstocks process for refining according to claim 2 is characterized in that, the described CO of taking off catalyzer is the C18 catalyzer.
5. propylene feedstocks process for refining according to claim 2 is characterized in that described hydrolytic catalyst of carbonyl sulfur is by active ingredient Cs
2O, K
2O, Na
2O, CaO, ZnO, BaO, MgO, Fe
2O
3In one or more, r-Al
2O
3Carrier or TiO
2The r-Al of modification
2O
3Complex carrier is formed; Described active component content is 1～40wt% of total catalyst weight.
6. propylene feedstocks process for refining according to claim 2 is characterized in that, described FeOOH desulfurizer obtains as follows:
(e), be to mix in 1: 2～1: 3 by iron and mol ratio hydroxy with solid ferrous compound and solid hydroxide;
(f) step (e) gained mixture is finished reaction by mixing to pinch, in described kneading process, the control temperature of charge is no more than 70 ℃;
(g) step (f) gained reaction product is dried in air;
(h) to washing of step (g) gained material and filtration;
(i) with step (h) gained solid seasoning or in 70 ℃～90 ℃ oven dry.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102653505A (en) * | 2011-03-04 | 2012-09-05 | 中国石油化工股份有限公司 | Propylene refining method |
| CN102992934A (en) * | 2011-09-17 | 2013-03-27 | 天华化工机械及自动化研究设计院有限公司 | Nitrogen closed-loop cyclic regeneration type propylene dehydration method and device |
| CN103087073A (en) * | 2011-10-28 | 2013-05-08 | 中国石油化工股份有限公司 | Preparation method of polyolefin resin nucleating agent |
| CN104452456A (en) * | 2014-11-20 | 2015-03-25 | 柳江县联华纸制品厂 | Water absorbent for papermaking |
| CN104689601A (en) * | 2015-02-27 | 2015-06-10 | 神华集团有限责任公司 | Propylene refining system and propylene refining method |
| CN107185496A (en) * | 2017-06-30 | 2017-09-22 | 山东益丰生化环保股份有限公司 | A kind of composite water absorbing agent and its preparation method and application |
| CN111354948A (en) * | 2020-03-27 | 2020-06-30 | 成都翊昂科技有限公司 | Ternary high-nickel positive electrode adhesive for lithium ion battery and preparation method thereof |
| CN111662153A (en) * | 2020-05-28 | 2020-09-15 | 实友化工（扬州）有限公司 | Propylene detoxification process of metal palladium adsorbent |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1702157A (en) * | 2005-05-02 | 2005-11-30 | 北京三聚环保新材料有限公司 | Method for refining catalytic liquefied petroleum gas |
| CN101077984A (en) * | 2007-07-25 | 2007-11-28 | 中国石油大学(北京) | Deep desulfurization method for liquefied petroleum gas |
-
2008
- 2008-05-29 CN CN200810113358.XA patent/CN101591215B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1702157A (en) * | 2005-05-02 | 2005-11-30 | 北京三聚环保新材料有限公司 | Method for refining catalytic liquefied petroleum gas |
| CN101077984A (en) * | 2007-07-25 | 2007-11-28 | 中国石油大学(北京) | Deep desulfurization method for liquefied petroleum gas |
Non-Patent Citations (4)
| Title |
|---|
| J. PETER WAKKER等: "High Temperature H2S and COS removal with MnO and FeO on gamma-Al2O3 Acceptors", 《IND. ENG. CHEM. RES.》 * |
| 冯续等: "国内外脱氧剂概述", 《化学工业与工程技术》 * |
| 况成承等: "炼厂气中丙烯精制工艺的选择", 《炼油设计》 * |
| 邹新禧: "《超强吸水剂》", 30 September 1991 * |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102653505A (en) * | 2011-03-04 | 2012-09-05 | 中国石油化工股份有限公司 | Propylene refining method |
| CN102653505B (en) * | 2011-03-04 | 2014-08-27 | 中国石油化工股份有限公司 | Propylene refining method |
| CN102992934A (en) * | 2011-09-17 | 2013-03-27 | 天华化工机械及自动化研究设计院有限公司 | Nitrogen closed-loop cyclic regeneration type propylene dehydration method and device |
| CN103087073A (en) * | 2011-10-28 | 2013-05-08 | 中国石油化工股份有限公司 | Preparation method of polyolefin resin nucleating agent |
| CN103087073B (en) * | 2011-10-28 | 2015-04-01 | 中国石油化工股份有限公司 | Preparation method of polyolefin resin nucleating agent |
| CN104452456A (en) * | 2014-11-20 | 2015-03-25 | 柳江县联华纸制品厂 | Water absorbent for papermaking |
| CN104689601A (en) * | 2015-02-27 | 2015-06-10 | 神华集团有限责任公司 | Propylene refining system and propylene refining method |
| CN107185496A (en) * | 2017-06-30 | 2017-09-22 | 山东益丰生化环保股份有限公司 | A kind of composite water absorbing agent and its preparation method and application |
| CN107185496B (en) * | 2017-06-30 | 2020-06-05 | 山东益丰生化环保股份有限公司 | Composite water absorbent, preparation method and application thereof |
| CN111354948A (en) * | 2020-03-27 | 2020-06-30 | 成都翊昂科技有限公司 | Ternary high-nickel positive electrode adhesive for lithium ion battery and preparation method thereof |
| CN111662153A (en) * | 2020-05-28 | 2020-09-15 | 实友化工（扬州）有限公司 | Propylene detoxification process of metal palladium adsorbent |
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| CN101591215B (en) | 2013-06-12 |
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