CN103992201A - Method for removal and cyclic utilization of DME in MTP technology and system thereof - Google Patents
Method for removal and cyclic utilization of DME in MTP technology and system thereof Download PDFInfo
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- CN103992201A CN103992201A CN201410194150.0A CN201410194150A CN103992201A CN 103992201 A CN103992201 A CN 103992201A CN 201410194150 A CN201410194150 A CN 201410194150A CN 103992201 A CN103992201 A CN 103992201A
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- dme
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention relates to a method for removal and cyclic utilization of DME in an MTP technology and a system thereof. The method comprises the following steps: materials from upstream, including methane, ethane, ethene, propylene, C3 hydrocarbon, C4<+>hydrocarbon and unreacted DME, enters a depropanizator to carry out distillation separation; a methanol solution is directly injected into the depropanizator to dissolve DME so as to evaporate methane, ethane, ethene, propylene and C3 hydrocarbon out of the top of the tower; C4<+>hydrocarbon and DME/methanol are distilled out of the bottom of the tower and enter an extraction separation tank; after separated from C4<+>hydrocarbon in the extraction separation tank, DME/methanol enters a methanol recovery tower; and refined DME/methanol evaporated from the methanol recovery tower is sent into a DME reactor to be recycled. The technological process is simple, and additional equipment is not required. Operation is simple. Methanol is directly injected into the depropanizator to efficiently dissolve DME and separate DME from propylene and C3; and DME/methanol is accumulated at the bottom of the tower and separated. Thus, purity of a propylene product is guaranteed. Through a simple extraction separation process, DME is recovered and returns the DME reactor to be recycled.
Description
Technical field
The method and the depropanizing tower system that the present invention relates to remove and recycle in a kind of preparing propylene from methanol (MTP) technique dme (DME), belong to Coal Chemical Industry, gas chemical industry field.
Background technology
Low-carbon alkene (ethene, propylene etc.) is as important basic chemical raw materials, the catalytic cracking/cracking of main source and petroleum naphtha, solar oil (all from oil).China's oil shortage of resources, petroleum import interdependency increases year by year, has limited to a certain extent the development of producing ethene and propylene product with petrochemical industry route.
The market has openings of China's ethene and propylene is larger, and at present, owing to being subject to the impact of ethane cracking ethene processed, the market has openings of domestic ethene dwindles gradually, and the market has openings of propylene is still very large.Only depend on propylene that petroleum cracking route produces to can not meet the demand in market far away, the new technology of therefore developing propylene enhancing is extremely urgent to expand propylene source, and preparing propylene from methanol technology is one of important method solving this present situation.
Mainly contain MTO and MTP by the Technology of preparing low carbon olefinic hydrocarbon with methanol.MTO (Methanol to Olefin) refers to by preparing low carbon olefinic hydrocarbon with methanol (ethene and propylene).MTP (Methanol to Propylene) refers to by methyl alcohol preparing propone.At present, two kinds of techniques have industrial applications, respectively have its advantage.Adopt these Technology preparing low-carbon olefins, as the important supplement means of traditional petrochemical industry route ethene processed, for the China of many coals, oil-poor, weak breath, will there is very important strategic importance.
The patented technology in this field of report is a lot of both at home and abroad at present, and as Chinese patent CN202246473, CN101050160A etc., mainly lay particular emphasis on MTP, MTO Technology aspect.What CN202246473 patent solved is the Moisture Content of propylene product, and CN101050160A patent discloses the alkene with 3 carbon atoms from having the method for separation of olefins of 4 carbon atoms.How dme in MTP technique (DME) removes and recycle this vital problem from propylene product but report.The boiling point of DME and propylene, propane approach, and are difficult to separate by traditional rectifying tower, if the propylene product of preparation is because containing DME impurity, are subject to huge restriction by making to prepare low-carbon alkene technology taking methyl alcohol as source, and the benefit of propylene product will greatly reduce.Develop the process of industrialization that a kind of process system simple, that DME removes and recycles efficiently can advance from aspects such as energy consumption, process cost, costs of equipment methanol-to-olefins technology.
Summary of the invention
The technical problem to be solved in the present invention is to provide the method and system that remove and recycle dme (DME) in a kind of simple preparing propylene from methanol (MTP) technique efficiently.The hydro carbons that wherein contains three carbon atoms in patent of the present invention is abbreviated as C3 hydrocarbon, and the hydro carbons that contains more than four carbon atom is abbreviated as C4
+hydrocarbon, DME/ methyl alcohol represents the mixing solutions of DME and methyl alcohol.The main nail alcohol of MTP technique (in DME reactor) under the effect of catalyzer generates DME, DME/ methyl alcohol (in MTP reactor) under the effect of MTP catalyzer generates the hydro carbons of different carbonatomss, hydro carbons separates and obtains propylene product, attached product ethene, LPG, gasoline products through rectifying tower.
For reaching above-mentioned purpose, in a kind of MTP technique of the present invention, remove, the method for recycle DME, containing methane, ethane, ethene, propylene, C3 hydrocarbon, C4+ hydrocarbon and unreacted DME material from upstream enters depropanizing tower and carries out rectifying separation, in depropanizing tower, directly inject dissolve with methanol solution DME, methane, ethane, ethene, propylene, C3 hydrocarbon are steamed from tower top, and C4+ hydrocarbon and DME/ methyl alcohol enter extracting and separating tank from distillating at the bottom of tower.In extracting and separating tank, DME/ methyl alcohol enters methanol distillation column after separating with C4+ hydrocarbon, and the refining DME/ methyl alcohol steaming through methanol distillation column is sent into DME reactor, in DME reactor, is DME by methanol conversion.The DME of dissolve with methanol and newly-generated DME enter MTP reactor as raw material, carry out cycling and reutilization, and reaction generates the hydro carbons of different carbonatomss.A C4+ hydrocarbon part is returned to MTP reactor as recycle hydrocarbons and is reacted, and another part is as LPG output of products.MTP reactor catalyst can generate small molecule hydrocarbon product by DME, C2～C6 hydrocarbon catalyzed reaction.
Further, method of the present invention, along with the growth in MTP reaction times, catalyst activity weakens gradually, and unconverted DME can enter in propylene product.When DME mass content in propylene product is greater than 5ppm, methyl alcohol starts to inject depropanizing tower; Method of the present invention, before methyl alcohol injects depropanizing tower, increases the reflux ratio of depropanizing tower tower top, until tower top steams in thing without C4
+till hydrocarbon, now fix reflux ratio (when depropanizing tower normal running, reflux ratio is greater than 1.8) and operate, if C4
+hydrocarbon content is too high, and first alcohol and water will steam and affect purified propylene from tower top.
Method of the present invention, before methyl alcohol injects depropanizing tower, adjusts service temperature and the working pressure of tower.According to the relative volatility difference of material, want to reach the separation requirement of C3 and C4+ hydrocarbon, the working pressure of tower and temperature have certain coupling requirement, and wherein the working pressure of preferred described depropanizing tower is 1.88～2.28MPaG, 95～120 DEG C of column bottom temperatures.
Method of the present invention, injects before depropanizing tower at methanol feedstock, stablize propylene tower operation, and regeneration protection bed using propylene tower overhead product line downstream as protector puts into operation.In regeneration protection bed, molecular sieve sorbent material is housed, can effectively absorbs DME, water and the methyl alcohol that in upstream product line propylene product, may sneak into.
Method of the present invention, directly between 10th～50 blocks of column plates of depropanizing tower, a tower tray progressively injects fresh methanol solution, increases gradually and injects quantity of methyl alcohol to normal operational settings flow (methanol feeding amount/depropanizing tower raw gas flow=0.1～0.3).Along with the increase of methyl alcohol injection rate, the regular content (methanol quality content is less than 3ppm) that constantly detects first alcohol and water in overhead product in depropanizing tower tower top sampling, and adjust at any time quantity of reflux and Ta Wen to ensure the stable operation of tower and to reach product separation requirement.
Method of the present invention, methyl alcohol/DME and C4+ hydrocarbon are gathered in the extracting and separating tank that enters in the lump downstream at the bottom of depropanizing tower tower.Extracting water at the bottom of methanol distillation column tower is injected from extracting and separating tank side, extracting water dissolves methyl alcohol/DME return methanol distillation column from separating tank bottom cycle, C4+ hydrocarbon separates from separating tank deck, and a part is returned to MTP reactor as recycle hydrocarbons, and a part is as LPG output of products.
The invention still further relates in a kind of MTP technique remove, the system of recycle DME, comprise depropanizing tower, deethanizing column, propylene tower, propylene product tank, extracting and separating tank, methanol distillation column, DME reactor and MTP reactor, wherein, the tower top discharge port of depropanizing tower is communicated with deethanizing column, propylene tower and the series connection of propylene product tank successively; At the bottom of the tower of depropanizing tower, discharge port is communicated with extracting and separating tank, methanol distillation column, DME reactor and MTP reactors in series successively; Described depropanizing tower is also provided with methanol feeding mouth.
System of the present invention, wherein also comprise overhead product on line analyzer, described overhead product on line analyzer is located between depropanizing tower and deethanizing column, and the opening for feed of on line analyzer and discharge port are communicated with the tower top discharge port of depropanizing tower, the opening for feed of deethanizing column respectively.
System of the present invention, wherein the working pressure of preferred described depropanizing tower is 1.88～2.28MPaG, 95～120 DEG C of column bottom temperatures.
System of the present invention; also comprise regeneration protection bed; described regeneration protection bed is located between propylene tower and propylene product tank; the opening for feed of regeneration protection bed and the discharge port of propylene tower are communicated with; the discharge port of regeneration protection bed and the opening for feed of propylene product tank are communicated with, DME, water and the methyl alcohol that may sneak into for absorbing propylene product.
System of the present invention, wherein at the bottom of preferred described methanol distillation column tower, a fluid inlet of liquid outlet and extracting and separating tank is communicated with.
The invention difference from existing technology is, the present invention injects methyl alcohol in depropanizing tower, the simple DME product that dissolves efficiently depropanizing tower top, DME/ methyl alcohol and C4
+hydrocarbon separates together at the bottom of tower.In extracting and separating tank, DME/ methyl alcohol separated with C4+ hydrocarbon and loop back DME reactor recycling by methanol distillation column.The present invention has: (1) technical process simply, does not need to increase extras, reduces facility investment expense; (2) simple to operate, directly inject methyl alcohol on depropanizing tower body top, high-efficiency dissolution DME, makes it to separate with propylene, C3, and DME/ methyl alcohol is isolated at the bottom of accumulating in tower, has ensured the purity of propylene product; (3) reclaim and return DME reactor recycling by simple extraction separation process.
Below in conjunction with accompanying drawing to removing in MTP technique of the present invention, the method and system of recycle DME is described further.
Brief description of the drawings
Fig. 1 be in MTP technique of the present invention, remove, the system flow schematic diagram of recycle DME.
Description of reference numerals: 1-depropanizing tower; 2-deethanizing column; 3-propylene tower; 4-regeneration protection bed; 5-propylene product tank; 6-extracting and separating tank; 7-methanol distillation column; 8-DME reactor; 9-MTP reactor; 10-on line analyzer; 11-is from the hydrocarbon gas charging of compressed element and debutylize tower top; The following light constituent of 12-C3 and C3; 13-C3 hydrocarbon, propylene; 14-propylene; 15-propylene product; 16-C4
+hydrocarbon, DME/ methyl alcohol; 17-DME/ methyl alcohol, extracting water; 18-DME/ methyl alcohol; 19-DME; The following light constituent of 20-C2 and C2; 21-C3 hydrocarbon and a small amount of C4
+hydrocarbon; 22-extracting water; 23-C4+ hydrocarbon; The hydrocarbon of the different carbonatomss of 24-; 31-methyl alcohol.
Embodiment
Be below embodiment and testing data etc. thereof, but content of the present invention is not limited to the scope of these embodiment.
Embodiment 1
As shown in Figure 1, in a kind of MTP technique of the present invention, remove, the method for recycle DME, enter depropanizing tower 1 rectifying from the hydrocarbon gas 11 of upstream compressed element and debutylize tower top.The following light constituent 12 of overhead product C3 hydrocarbon and C3 obtains qualified propylene product through deethanizing column 2, propylene tower 3 and regeneration protection bed 4.Wherein, deethanizing column 2 tower tops are isolated C2 and the following light constituent 20 of C2, and deethanizing column 2 materials at bottom of towers are sent into propylene tower 3 and isolated propylene 14 and C3 hydrocarbon and a small amount of C4
+hydrocarbon 21, propylene 14 is sent into regeneration protection bed 4 and is absorbed DME, water and the methyl alcohol that may sneak into and obtain qualified propylene product 15 and send into propylene product tank 5 and store.
In the time that overhead product C3 and the following light constituent 12 of C3 contain more DME, directly between 10～50 blocks of column plates of depropanizing tower, progressively inject fresh methanol 31 solution, constantly adjust the flow that injects methyl alcohol, thereby in regular detection overhead product, the content of first alcohol and water determines methyl alcohol injection rate.Methyl alcohol (is C4 at the bottom of DME is dissolved in to depropanizing tower
+hydrocarbon, DME/ methyl alcohol 16) enter extracting and separating tank 6.In extracting and separating tank 6, isolate DME/ methyl alcohol, water 17 and C4
+hydrocarbon, C4
+hydrocarbon is sent into downstream unit processing, and DME/ methyl alcohol, water 17 are sent into methanol distillation column 7.The extracting water cycle at 7 ends of methanol distillation column is injected extracting and separating tank 6 and is dissolved methyl alcohol and DME, and together inject methanol distillation column 7, methyl alcohol/the DME18 distilling out is as the raw material of DME reactor 8, the DME of methanol conversion and the DME19 of dissolve with methanol enter MTP reactor 9 as raw material in the lump and generate the hydrocarbon of different carbonatomss, thereby have realized circulation and the recycling of unreacted DME.
Taking a MTP device of producing 500000 tons/year of propylene per year as example, depropanizing tower charging 11 flows are 120000-140000kg/h, contain methane, ethane, ethene, C3 hydrocarbon, propylene, C4 in charging
+hydrocarbon etc.Methyl alcohol injects before depropanizing tower: increase first gradually the quantity of reflux of depropanizing tower 1 tower top, be increased to 250000～400000kg/h, when the on line analyzer 10 of overhead product detects without C4
+when hydrocarbon, stablizing quantity of reflux operates; The regeneration protection bed 4 in propylene tower top product line downstream is put into operation; Enter the 6 operation operations of extracting and separating tank for extracting DME/ methyl alcohol from 7 extracting water cycle at the bottom of methanol distillation column, the flow of extracting water is 70000～90000kg/h; The working pressure of depropanizing tower is made as 1.88～2.28MPaG; Adjust depropanizing tower column bottom temperature to 95～120 DEG C; Start to inject slowly methyl alcohol, the flow of methyl alcohol can be adjusted flexibly, and methyl alcohol flow is 20000～450000kg/h, and regular constantly at tower top sampling detection water and methanol content, and adjusts gradually quantity of reflux and Ta Wen; DME and methyl alcohol enter extracting and separating tank 6 and C4 at the bottom of accumulating in depropanizing tower 1 tower
+hydrocarbon separates and enters methanol distillation column 7, after refining, returns in DME reactor 8, and methyl alcohol reacts raw DME under catalyst action, and DME enters the lighter hydrocarbons of MTP reactor generation low carbon atom number.
Embodiment 2
As shown in Figure 1, in a kind of MTP technique of the present invention, remove, the system of recycle DME, comprise depropanizing tower 1, deethanizing column 2, propylene tower 3, propylene product tank 5, extracting and separating tank 6, methanol distillation column 7, DME reactor 8, wherein, the tower top discharge port of depropanizing tower 1 is communicated with deethanizing column 2, propylene tower 3 and 5 series connection of propylene product tank successively; At the bottom of the tower of depropanizing tower 1, discharge port is communicated with extracting and separating tank 6, methanol distillation column 7, DME reactor 8 and 9 series connection of MTP reactor successively; Described depropanizing tower 1 is also provided with methanol feeding mouth.Also be provided with overhead product on line analyzer 10 for detection of C4
+hydrocarbon content, this On-line Product analyser 10 is located between depropanizing tower 1 and deethanizing column 2, and its opening for feed and discharge port are communicated with the tower top discharge port of depropanizing tower 1, the opening for feed of deethanizing column 2 respectively.Between propylene tower 3 and propylene product tank 5, be also provided with regeneration protection bed 4; the opening for feed of regeneration protection bed 4 and the discharge port of propylene tower 3 are communicated with; the discharge port of regeneration protection bed 4 and the opening for feed of propylene product tank 5 are communicated with, DME, water and the methyl alcohol that may sneak into for absorbing propylene product.Wherein, at the bottom of methanol distillation column 7 towers, a fluid inlet of liquid outlet and extracting and separating tank 6 is communicated with, and dissolves methyl alcohol and DME for the extracting water cycle at 7 ends of methanol distillation column is injected to extracting and separating tank 6.The working pressure of described depropanizing tower 1 is preferably 1.88～2.28MPaG, and column bottom temperature is preferably 95～120 DEG C.
Above-described embodiment is described the preferred embodiment of the present invention; not scope of the present invention is limited; design under the prerequisite of spirit not departing from the present invention; various distortion and improvement that those of ordinary skill in the art make technical scheme of the present invention, all should fall in the definite protection domain of the claims in the present invention book.
Claims (11)
1. in MTP technique, remove, a method of recycle DME, it is characterized in that: contain methane, ethane, ethene, propylene, C3 hydrocarbon, C4 from upstream
+hydrocarbon and unreacted DME material enter depropanizing tower and carry out rectifying separation, in depropanizing tower, directly inject dissolve with methanol solution DME, methane, ethane, ethene, propylene, C3 hydrocarbon are steamed, C4 from tower top
+hydrocarbon and DME/ methyl alcohol enter extracting and separating tank from distillating at the bottom of tower; In extracting and separating tank, DME/ methyl alcohol and C4
+hydrocarbon enters methanol distillation column after separating, and the refining DME/ methyl alcohol steaming through methanol distillation column is sent into DME reactor and carried out cycling and reutilization.
2. method according to claim 1, is characterized in that: increase the quantity of reflux of depropanizing tower tower top, until tower top steams C4 in thing
+till hydrocarbon content maybe cannot detect lower than the detection lower limit of analysis meter.
3. method according to claim 1, is characterized in that: the working pressure of described depropanizing tower is 1.88～2.28MPaG, 95～120 DEG C of column bottom temperatures.
4. method according to claim 1; it is characterized in that: before methanol feedstock injects depropanizing tower; stablize propylene tower operation, and regeneration protection bed using propylene tower overhead product line downstream as protector puts into operation, absorb DME, water and the methyl alcohol that in propylene product, may sneak into.
5. method according to claim 1, is characterized in that: the extracting water at the bottom of methanol distillation column tower is injected to extracting and separating tank, in order to extract DME/ methyl alcohol.
6. method according to claim 1, is characterized in that: directly between 10～50 blocks of column plates of depropanizing tower, progressively inject fresh methanol solution, constantly adjust the flow that injects methyl alcohol, the content of first alcohol and water in regular detection overhead product.
7. in a MTP technique, remove, the system of recycle DME, comprise depropanizing tower, deethanizing column, propylene tower, propylene product tank, extracting and separating tank, methanol distillation column, DME reactor and MTP reactor, wherein, the tower top discharge port of depropanizing tower is communicated with deethanizing column, propylene tower and the series connection of propylene product tank successively; At the bottom of the tower of depropanizing tower, discharge port is communicated with extracting and separating tank, methanol distillation column, DME reactor and MTP reactors in series successively; Described depropanizing tower is also provided with methanol feeding mouth.
8. system according to claim 7, it is characterized in that: also comprise overhead product on line analyzer, described overhead product on line analyzer is located between depropanizing tower and deethanizing column, and the opening for feed of on line analyzer and discharge port are communicated with the tower top discharge port of depropanizing tower, the opening for feed of deethanizing column respectively.
9. system according to claim 7, is characterized in that: the working pressure of described depropanizing tower is 1.88～2.28MPaG, 95～120 DEG C of column bottom temperatures.
10. system according to claim 7; it is characterized in that: also comprise regeneration protection bed; described regeneration protection bed is located between propylene tower and propylene product tank; the opening for feed of regeneration protection bed and the discharge port of propylene tower are communicated with; the discharge port of regeneration protection bed and the opening for feed of propylene product tank are communicated with, DME, water and the methyl alcohol that may sneak into for absorbing propylene product.
11. systems according to claim 7, is characterized in that: at the bottom of described methanol distillation column tower, a fluid inlet of liquid outlet and extracting and separating tank is communicated with.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410194150.0A CN103992201B (en) | 2014-05-08 | 2014-05-08 | Remove in MTP technique, the method and system of recycle DME |
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|---|---|---|---|
| CN201410194150.0A CN103992201B (en) | 2014-05-08 | 2014-05-08 | Remove in MTP technique, the method and system of recycle DME |
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| CN103992201B CN103992201B (en) | 2015-12-02 |
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| CN105439800A (en) * | 2015-12-30 | 2016-03-30 | 神华集团有限责任公司 | System and method for removing DME (dimethyl ether) in MTP (methanol to propylene) products |
| CN106478342A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | The method that material benzenemethanol removes DME in product is utilized in MTP technique |
| CN107721829A (en) * | 2016-08-12 | 2018-02-23 | 惠生工程（中国）有限公司 | A kind of method that dimethyl ether is removed from the feed stream comprising propane and dimethyl ether |
| CN112533888A (en) * | 2018-08-10 | 2021-03-19 | 环球油品有限责任公司 | Process for reducing oxygenate recycle in MTO conversion |
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| CN112533888A (en) * | 2018-08-10 | 2021-03-19 | 环球油品有限责任公司 | Process for reducing oxygenate recycle in MTO conversion |
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| Publication number | Publication date |
|---|---|
| CN103992201B (en) | 2015-12-02 |
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