CN101591215B - Normal-temperature propylene refining technology and water absorbent used therein - Google Patents
Normal-temperature propylene refining technology and water absorbent used therein Download PDFInfo
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Abstract
The invention relates to water absorbent which can be used for a propylene material refining technology. The water absorbent is one or a plurality of crosslinking acrylate, vinyl alcohol-acrylate segmented copolymer, modified PVA, polyacrylamide, quadripolymer composed of starch-grafted acrylate, starch, crylic acid acide-acrylamide and maleic anhydride, cellulose-grafted acrylate, starch-grafted acrylonitrile saponification hydrolysate and deformed polyvinyl alcohol, or the water absorbent is the mixture of above one or a plurality of components and one or a plurality of solid alkali, A-shaped molecular sieve and aluminum oxide. The invention also discloses a propylene material refining technology which uses the water absorbent with high dewatering capacity and desulfurater with high sulfur capacity on the basis of the above water absorbent, improves propylene refining ability as a whole, can satisfy the demands of long period and high-load operation of a propylene refining device, and has high refining efficiency.
Description
Technical field
The present invention relates to a kind of water-retaining agent and use the normal-temperature propylene refining technique of this water-retaining agent, belong to the propylene refining technical field.
Background technology
The polypropylene synthesis technique is take propylene as raw material, under catalyst action, generates organic high molecular polymer through polyreaction.In the polypropylene synthesis technique, except the perfect of process for refining itself with effectively controlling, quality control to propylene feedstocks is also vital, because if the detrimental impurity content in propylene feedstocks is high, will affect activity and the orientation property of catalyzer, even cause poisoning of catalyst that polyreaction can not be occured, and then affect quality product.
Liquid propylene process for refining route at present commonly used mainly comprises three kinds:
The 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;
The 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 propylene feedstocks comprises water, sulfide, CO and oxygen etc.Take off CO and dearsenification for propylene feedstocks is refining, commonly used in the market is carbon monoxide in C18 catalyst removal propylene, and 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 a certain amount of arsenic of dearsenic agent absorption, the dearsenification ability descends, and in propylene, arsenic content improves, and will note changing dearsenic agent this moment.The 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 manganese series catalyzer.Because BH type reductor cost is high, so the propylene feedstocks process for refining is selected manganese deoxidier (take MnO, MnO+FeO etc. as active ingredient) 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, propylene etc., has the higher deoxidation degree of depth, deoxidation capacity and activity.In addition, Chinese patent literature CN200610113865.4 discloses a kind of Mn-Ag double activated component reductor, and reductor is with Mn
3O
4Be main active component, therein contained a small amount of Ag
2Under the katalysis of O, decrease Mn
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 room temperature, the micro amount of oxygen in ethene, propylene etc. is purified to 0.05ppm, the reductor of this invention is used for polyolefin industry and produces, can extend the reductor regeneration period, avoid polymerizing catalyst poisoning, reduce production costs, have obvious economic benefit.
For crude propylene, because the content of wherein water and sulfide is larger, so the refining emphasis of propylene feedstocks is dehydration and desulfurization.Water in propylene feedstocks can with catalyzer and activator generation vigorous reaction, thereby make catalyst activity reduction; During higher than 100ug/g, propylene polymerization can not occur when water-content; Sulphur in propylene feedstocks can make the polyreaction chain termination on the one hand, can make catalyst activity reduction on the other hand, even stops up still thereby cause the plasticizing piece occurring in polyolefine production declining, degree of isotacticity decline, powder, affects production process and production efficiency.
In prior art, under the condition of normal temperature, certain pressure, in propylene refining technique, dehydration technique commonly used is mainly to adopt solid alkali, aluminum oxide or molecular sieve as water-retaining agent.Wherein, choice for use propylene refining solid caustic soda tower dewaters to propylene feedstocks, owing to also having the part acidic components in 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; In this part solid alkali of use carries out dehydration, because moisture in the propylene feedstocks system is larger, and mostly be free-water, after can't all condensing, this part water normally removes 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.Liquid caustic soda liquid level superelevation after time is long is flooded opening for feed, and at first propylene feedstocks can pass the liquid caustic soda layer in the solid caustic soda tower so, the portable propylene of bringing into of sulfur-containing impurities wherein, and easily cause alkali lye to be carried into the molecular sieve tower, and cause the molecular sieve tower to lose efficacy, can't dewater.In addition, if use aluminum oxide or molecular sieve to dewater, dehydration finite capacity due to 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, therefore it is easy to reach capacity, so need often switch the operating process of drying chamber, discharging propylene, nitrogen replacement, nitrogen temperature regeneration, thereby cause propylene discharging torch pipe network amount to increase, recirculated water, nitrogen, electricity etc. consumptions increase, and are more importantly to have increased the device operation cost.Similarly, the solid caustic soda water-intake rate can not reach 15% of own wt, but also is easy to deliquescence, so the problems referred to above are also the technical problems that exists when using solid alkali.
Sulphur in propylene to removing of this partial vulcanization thing, at first need to be converted into organosulfur inorganic sulfur (H mainly take organosulfur (carbonylsulfide COS) as main under the hydrolytic reagent effect
2S), then use sweetening agent that inorganic sulfur is removed.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, the sweetening effectiveness of sweetening agent just begins to occur downtrending, and just should in time change sweetening agent this moment.At present propylene feedstocks sweetening agent commonly used comprises the sweetening agent take zinc oxide or cupric oxide as 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 comprised 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 5% left and right.Chinese patent literature CN00114588.6 discloses a kind of sweetening agent that can be used for the fine desulfurizing technology of the production technique such as synthetic polypropylene, and this sweetening agent is comprised 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, in prior art, the Sulfur capacity of propylene refining sweetening agent commonly used is all very low.For propylene refining technique, 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 need the high sweetening agent of Sulfur capacity in the propylene feedstocks process for refining.
Summary of the invention
It is the low problem of water-retaining agent dehydration capacity in the propylene feedstocks process for refining in 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 frequent constantly water-retaining agent that can be used for propylene refining of regeneration.
It is that in of the prior art third rare process for refining, the sweetening agent Sulfur capacity is lower that the present invention will solve second technical problem, need constantly to regenerate to water-retaining agent and change sweetening agent, cause the low problem of purification efficiency, and then providing 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.
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 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 thing, one or more in the distortion polyvinyl alcohol, or one or more and solid alkali in above-mentioned substance, A type molecular sieve, the mixture of one or more in 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) fill water-retaining agent in dehydration reactor, described water-retaining agent be crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, Modified PVA, polyacrylamide, starch grafted acrylate, starch, acrylic acid acrylamide, along in acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification thing, distortion polyvinyl alcohol one or more, or one or more the mixture in one or more and solid alkali in above-mentioned substance, A type molecular sieve, 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 processes;
(c) propylene after taking off CO and processing 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 the cos hydrolysis reactor that is filled with respectively hydrolytic catalyst of carbonyl sulfur and the desulphurization reactor that is filled with sweetening agent successively, described sweetening agent is FeOOH desulfurizer, and this sweetening agent comprises the hydrous iron oxide of 30～60wt%; Be 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 in temperature of reaction
-1Condition under, propylene feedstocks is carried out desulfurization processes.
In aforesaid propylene feed purification technique, 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 technique, 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 forms; Described active component content is 1～40wt% of total catalyst weight.
Wherein, described FeOOH desulfurizer obtains as follows:
(e) with solid ferrous compound and solid hydroxide, be to mix in 1: 2～1: 3 by iron and mol ratio hydroxy;
(f) step (e) gained mixture is completed reaction by kneading, in described kneading process, control temperature of charge and be no more than 70 ℃;
(g) step (f) gained reaction product is dried in air;
(h) step (g) gained material is washed and filtered;
(i) with step (h) gained solid seasoning or in 70 ℃～90 ℃ oven dry.
The present invention has advantages of as described below:
(1) in 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, Modified PVA, polyacrylamide, starch grafted acrylate, starch, acrylic acid acrylamide, along in acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification thing, distortion polyvinyl alcohol one or more, or one or more the mixture in one or more and solid alkali in above-mentioned substance, A type molecular sieve, aluminum oxide; This water-retaining agent has larger 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 that nitrogen temperature is regenerated, reduce on the whole process for refining running cost, improved purification efficiency;
(2) use FeOOH desulfurizer to remove sulfide in propylene in 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 the sweetening agent with high Sulfur capacity have been used in propylene feedstocks process for refining of the present invention, acting in conjunction by said two devices, improved on the whole the propylene refining ability, more can satisfy propylene refining device long period, heavy-duty service, processing by this technique can be brought up to the high-quality level with the quality of propylene feedstocks, and purification efficiency is very high.
Embodiment
The FeOOH desulfurizer that uses in propylene feedstocks process for refining of the present invention is special, 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, thereby kneading 3h completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards, be beneficial to fully completing of above-mentioned reaction.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after washing and filtering is dried, and bake out temperature is 80 ℃, and drying time is 3h, can make amorphous FeOOH desulfurizer required in propylene refining technique 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, thereby kneading 0.5h completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after 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 propylene refining technique 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, thereby kneading 1.0h completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after washing and filtering is carried out seasoning, and drying temperature is 45 ℃, and drying time is 3h, can make amorphous FeOOH desulfurizer required in propylene refining technique 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, thereby kneading 15min completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after washing and filtering is dried, and bake out temperature is 90 ℃, and drying time is 3h, can make amorphous FeOOH desulfurizer required in propylene refining technique 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, thereby kneading 2.0h completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after 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 propylene refining technique 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, thereby kneading 25min completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after 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 propylene refining technique 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, thereby kneading 30min completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after washing and filtering is dried, and bake out temperature is 100 ℃, and drying time is 1h, can make amorphous FeOOH desulfurizer required in propylene refining technique 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, thereby kneading 30min completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after 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 propylene refining technique 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, thereby kneading 30min completes the solid state reaction between above-mentioned reactant, above-mentioned reaction product is placed in air dries afterwards.
Material after drying first adds water and stirs, and repetitive scrubbing uses whizzer that above-mentioned washings is filtered till the gained filtrate sulfate radical-free (usually checking with bariumchloride).
Above-mentioned solid after 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 propylene refining technique of the present invention.
In above-described embodiment 1～9, the ferrous sulfate powder that uses is FeSO
47H
2O content is the industrial raw material of 88～90wt%; In sodium hydroxide in the content of NaOH or potassium hydroxide the content of KOH be 90～93wt%; Baking step carries out in electric drying oven with forced convection; The model of the kneader that uses is the polyfunctional catalyst forming machine 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 dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 30wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed.After above-mentioned process for refining in 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 dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 40wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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.
Embodiment12
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 dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 10 ℃, pressure is 1.0Mpa, and the air speed by the dehydrogenation catalyst bed is 0.5h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O and TiO
2The r-Al of modification
2O
3Complex carrier forms, wherein active component content is the 10wt% of this hydrolyst gross weight, this hydrolyst is packed in 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 50wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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 dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 60wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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 dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 70wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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 dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. taking the 30g active ingredient is the nickel deoxidier of NiO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 50 ℃, and 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 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 80wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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 thing as dewatering agent, and it is packed in dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take the 30g hydrolytic catalyst of carbonyl sulfur, this hydrolyst is by K
2O, MgO and TiO
2The r-Al of modification
2O
3Complex carrier forms, wherein active component content is the 30wt% of this hydrolyst gross weight, this hydrolyst is packed in 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 80wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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: 1. select the mixture of 20g starch grafted acrylate and solid alkali as dewatering agent, and it is packed in dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 85wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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: 1. select the mixture of 20g Modified PVA and aluminum oxide as dewatering agent, and it is packed in dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 90wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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: 1. select the mixture of 20g polyacrylamide and solid alkali as dewatering agent, and it is packed in dehydration reactor, the temperature of reaction of setting in 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 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 processes; 3. take the manganese deoxidier that the 30g active ingredient is MnO and FeO, it is packed in deoxidation reactor, and the temperature of reaction of setting this reactor is 30 ℃, pressure is 1.3Mpa, and the air speed by the dehydrogenation catalyst bed is 2.0h
-1, propylene feedstocks is carried out deoxidation treatment; 4. take 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 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 propylene feedstocks is hydrolyzed; 5. to take 30g hydroxyl oxidize iron level be the sweetening agent of 90wt% and it is packed in desulphurization reactor, and 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 propylene feedstocks is removed; 6. take 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 in rear propylene 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 mentioning in above-described embodiment, 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 thing, distortion polyvinyl alcohol A, or one or more the mixture in one or more and solid alkali in above-mentioned substance, A type molecular sieve, aluminum oxide; Arbitrary combination between above-mentioned substance all is applicable to the present invention.
Although the present invention elaborates it by above-mentioned specific embodiment; but; those skilled in the art should be understood that any form that does not exceed the claim protection domain made on this basis and the variation of details, all belong to invention which is intended to be protected.
Claims (5)
1. propylene feedstocks process for refining, it comprises the steps:
(a) fill water-retaining agent in dehydration reactor, described water-retaining agent be in crosslinked salt polyacrylate, vinyl alcohol-acrylate segmented copolymer, Modified PVA, polyacrylamide, starch grafted acrylate, starch and vinylformic acid, acrylamide and the tetrapolymer that forms along acid anhydrides, cellulose graft acrylate, starch-grafted vinyl cyanide saponification thing one or more, or one or more the mixture in one or more and solid alkali in above-mentioned substance, A type molecular sieve, 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, are 0.5 ~ 5.0h by the volume space velocity that takes off the CO beds in temperature of reaction
-1Condition under, propylene feedstocks is taken off CO processes;
(c) propylene after taking off CO and processing 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 the 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 FeOOH desulfurizer, and this sweetening agent comprises the hydrous iron oxide of 30 ~ 90wt%; Be 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 in temperature of reaction
-1Condition under, propylene feedstocks is carried out desulfurization processes.
2. propylene feedstocks process for refining according to claim 1, 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 ~ 5.0h in temperature of reaction
-1Condition under, propylene feedstocks is carried out deep dehydration.
3. propylene feedstocks process for refining according to claim 1, is characterized in that, the described CO of taking off catalyzer is the C18 catalyzer.
4. propylene feedstocks process for refining according to claim 1, 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 forms; Described active component content is 1 ~ 40wt% of total catalyst weight.
5. propylene feedstocks process for refining according to claim 1, is characterized in that, described FeOOH desulfurizer obtains as follows:
(e) with solid ferrous compound and solid hydroxide, be that 1:2 ~ 1:3 mixes by iron and mol ratio hydroxy;
(f) step (e) gained mixture is completed reaction by kneading, in described kneading process, control temperature of charge and be no more than 70 ℃;
(g) step (f) gained reaction product is dried in air;
(h) step (g) gained material is washed and filtered;
(i) with step (h) gained solid seasoning or in 70 ℃ ~ 90 ℃ oven dry.
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| 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 |
| 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 |
| CN104689601B (en) * | 2015-02-27 | 2017-11-14 | 神华集团有限责任公司 | Propylene refining system and propylene refining method |
| 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 |
| CN111354948B (en) * | 2020-03-27 | 2021-04-27 | 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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