CN103992201B - Remove in MTP technique, the method and system of recycle DME - Google Patents
Remove in MTP technique, the method and system of recycle DME Download PDFInfo
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- CN103992201B CN103992201B CN201410194150.0A CN201410194150A CN103992201B CN 103992201 B CN103992201 B CN 103992201B CN 201410194150 A CN201410194150 A CN 201410194150A CN 103992201 B CN103992201 B CN 103992201B
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- dme
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- methyl alcohol
- propylene
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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 present invention relates in a kind of MTP technique remove, the method and system of recycle DME, contain methane, ethane, ethene, propylene, C3 hydrocarbon, C4 from upstream
+hydrocarbon and unreacted DME material enter depropanizing tower and carry out rectifying separation, directly inject dissolve with methanol solution DME, methane, ethane, ethene, propylene, C3 hydrocarbon are steamed from tower top, C4 in depropanizing tower
+hydrocarbon and DME/ methyl alcohol distillate and enter extracting and separating tank at the bottom of tower; In extracting and separating tank, DME/ methyl alcohol and C4
+hydrocarbon enters methanol distillation column after being separated, and the refining DME/ methyl alcohol feeding DME reactor steamed through methanol distillation column carries out cycling and reutilization.Present invention process flow process simply, does not need to increase extras; Simple to operate, directly in depropanizing, inject methyl alcohol, high-efficiency dissolution DME is separated with propylene, C3, and DME/ methyl alcohol accumulates at the bottom of tower and isolates, and ensures the purity of propylene product; Reclaimed by simple extraction separation process and return DME reactor recycling.
Description
Technical field
The present invention relates to the method and depropanizing tower system that remove and recycle dme (DME) in a kind of preparing propylene from methanol (MTP) technique, belong to Coal Chemical Industry, gas chemical industry field.
Background technology
Low-carbon alkene (ethene, propylene etc.) 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, limits the development of producing ethene and propylene product with petrochemical industry route to a certain extent.
The market has openings of China's ethene and propylene is comparatively large, and at present, due to the impact by ethane cracking ethene, the market has openings of domestic ethene reduces gradually, and the market has openings of propylene is still very large.The propylene only produced by petroleum cracking route can not meet the demand in market far away, and the new technology 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.
MTO and MTP is mainly contained by the Technology of preparing low carbon olefinic hydrocarbon with methanol.MTO (MethanoltoOlefin) refers to by preparing low carbon olefinic hydrocarbon with methanol (ethene and propylene).MTP (MethanoltoPropylene) 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, for many coals, oil-poor, weak breath China 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, as Chinese patent CN202246473, CN101050160A etc., mainly lays 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 the method for separation of olefins with 4 carbon atoms.In MTP technique, how dme (DME) removes and recycle this vital problem from propylene product does not but have report.The boiling point of DME and propylene, propane are close, are difficult to be separated by traditional rectifying tower, if the propylene product of preparation is because of containing DME impurity, be that source is prepared low-carbon alkene technology and is subject to huge restriction with methyl alcohol by making, the benefit of propylene product will greatly reduce.Developing a kind of simple, that DME removes and recycles efficiently process system can from the process of industrialization of the aspect propelling methanol-to-olefins technology such as energy consumption, process cost, cost of equipment.
Summary of the invention
The technical problem to be solved in the present invention is to provide the method and system removing and recycle dme (DME) in a kind of simple preparing propylene from methanol (MTP) technique efficiently.Hydro carbons wherein containing three carbon atoms in patent of the present invention is abbreviated as C3 hydrocarbon, and the hydro carbons containing more than four carbon atoms 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 carbonatoms, hydro carbons is separated through rectifying tower and obtains propylene product, attached product ethene, LPG, gasoline products.
For reaching above-mentioned purpose, remove in a kind of MTP technique of the present invention, the method for recycle DME, contain methane, ethane, ethene, propylene, C3 hydrocarbon, C4+ hydrocarbon and unreacted DME material from upstream to enter depropanizing tower and carry out rectifying separation, directly dissolve with methanol solution DME is injected in depropanizing tower, methane, ethane, ethene, propylene, C3 hydrocarbon are steamed from tower top, and C4+ hydrocarbon and DME/ methyl alcohol distillate and enter extracting and separating tank at the bottom of tower.In extracting and separating tank, DME/ methyl alcohol enters methanol distillation column after being separated with C4+ hydrocarbon, and the refining DME/ methyl alcohol steamed through methanol distillation column sends into DME reactor, is DME in DME reactor by methanol conversion.DME and the newly-generated DME of dissolve with methanol enter MTP reactor as raw material, carry out cycling and reutilization, and reaction generates the hydro carbons of different carbonatoms.A C4+ hydrocarbon part returns MTP reactor as recycle hydrocarbons and reacts, and another part is as LPG output of products.DME, C2 ~ C6 hydrocarbon catalyzed reaction can be generated small molecule hydrocarbon product by MTP reactor catalyst.
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 in propylene product, DME mass content 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 (during depropanizing tower normal running, reflux ratio is greater than 1.8) and operate, if C4
+hydrocarbon content is too high, then first alcohol and water will steam from tower top affects purified propylene.
Method of the present invention, before methyl alcohol injects depropanizing tower, the service temperature of adjustment tower and working pressure.According to the relative volatility difference of material, want the separation requirement reaching C3 and C4+ hydrocarbon, the working pressure of tower and temperature have necessarily mates requirement, and wherein the working pressure of preferred described depropanizing tower is 1.88 ~ 2.28MPaG, column bottom temperature 95 ~ 120 DEG C.
Method of the present invention, before methanol feedstock injects depropanizing tower, stablizes propylene tower operation, and is put into operation by the regeneration protection bed of propylene tower overhead product line downstream as protector.Regeneration protection bed, built with molecular sieve sorbent material, effectively can absorb DME, water and the methyl alcohol that may be mixed in upstream product line propylene product.
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) constantly detecting first alcohol and water in overhead product in the sampling of depropanizing tower tower top, and adjust quantity of reflux and Ta Wen at any time to ensure the stable operation of tower and to reach product separation requirement.
Method of the present invention, methyl alcohol/DME and C4+ hydrocarbon is gathered in the extracting and separating tank entering downstream at the bottom of depropanizing tower tower in the lump.Extracting water at the bottom of methanol distillation column tower is injected from extracting and separating tank side, methyl alcohol/DME dissolves and loop back methanol distillation column bottom separating tank by extracting water, C4+ hydrocarbon separates from separation tank deck, and a part returns 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 successively with deethanizing column, propylene tower and propylene product tank serial communication; Discharge port at the bottom of the tower of depropanizing tower is communicated with MTP reactors in series with extracting and separating tank, methanol distillation column, DME reactor 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 is communicated with the tower top discharge port of depropanizing tower, the opening for feed of deethanizing column respectively with discharge port.
System of the present invention, wherein the working pressure of preferred described depropanizing tower is 1.88 ~ 2.28MPaG, column bottom temperature 95 ~ 120 DEG C.
System of the present invention; also comprise regeneration protection bed; described regeneration protection bed is located between propylene tower and propylene product tank; the regeneration protection opening for feed of bed is communicated with the discharge port of propylene tower; the discharge port of regeneration protection bed is communicated with the opening for feed of propylene product tank, for absorbing DME, water and the methyl alcohol that may be mixed in propylene product.
System of the present invention, wherein at the bottom of preferred described methanol distillation column tower, liquid outlet is communicated with a fluid inlet of extracting and separating tank.
The invention difference from existing technology is, the present invention injects methyl alcohol in depropanizing tower, the simple DME product dissolving depropanizing tower top efficiently, DME/ methyl alcohol and C4
+hydrocarbon separates together at the bottom of tower.In extracting and separating tank, DME/ methyl alcohol is separated with C4+ hydrocarbon and is looped back DME reactor by methanol distillation column and recycle.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 at depropanizing tower body upper part, high-efficiency dissolution DME, make it to be separated with propylene, C3, DME/ methyl alcohol accumulates at the bottom of tower and isolates, and ensure that the purity of propylene product; (3) reclaimed by simple extraction separation process and return DME reactor recycling.
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.
Accompanying drawing explanation
Fig. 1 be remove in MTP technique of the present invention, 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; 12-C3 and below C3 light constituent; 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; 20-C2 and below C2 light constituent; 21-C3 hydrocarbon and a small amount of C4
+hydrocarbon; 22-extracting water; 23-C4+ hydrocarbon; The hydrocarbon of the different carbonatoms 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 embodiments.
Embodiment 1
As shown in Figure 1, to remove, the method for recycle DME in a kind of MTP technique of the present invention, the hydrocarbon gas 11 from stream compression unit and debutylize tower top enters depropanizing tower 1 rectifying.Overhead product C3 hydrocarbon and below C3 light constituent 12 obtain qualified propylene product through deethanizing column 2, propylene tower 3 and regeneration protection bed 4.Wherein, deethanizing column 2 tower top isolates C2 and below C2 light constituent 20, and deethanizing column 2 materials at bottom of tower is 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 be mixed into and obtain qualified propylene product 15 and send into propylene product tank 5 and store.
When overhead product C3 and below C3 light constituent 12 is containing more DME, directly between 10 ~ 50 blocks of column plates of depropanizing tower, progressively inject fresh methanol 31 solution, the flow of methyl alcohol is injected in continuous adjustment, in regular detection overhead product first alcohol and water content thus determine methyl alcohol injection rate.DME is dissolved in (i.e. C4 at the bottom of depropanizing tower by methyl alcohol
+hydrocarbon, DME/ methyl alcohol 16) enter extracting and separating tank 6.DME/ methyl alcohol, water 17 and C4 is isolated in extracting and separating tank 6
+hydrocarbon, C4
+hydrocarbon sends into downstream unit process, and DME/ methyl alcohol, water 17 send into methanol distillation column 7.The extracting water cycle at methanol distillation column 7 end 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 distilled out is as the raw material of DME reactor 8, the DME of methanol conversion and the DME19 of dissolve with methanol enters as raw material the hydrocarbon that MTP reactor 9 generates different carbonatoms in the lump, thus achieves circulation and the recycling of unreacted DME.
Produce the MTP device of 500,000 tons/year of propylene per year for one, depropanizing tower charging 11 flow is 120000-140000kg/h, containing methane, ethane, ethene, C3 hydrocarbon, propylene, C4 in charging
+hydrocarbon etc.Before methyl alcohol injects depropanizing tower: the quantity of reflux increasing depropanizing tower 1 tower top first gradually, is increased to 250000 ~ 400000kg/h, when the on line analyzer 10 of overhead product detects without C4
+stablize quantity of reflux when hydrocarbon to operate; The regeneration in propylene tower top product line downstream protection bed 4 is put into operation; From at the bottom of methanol distillation column 7 extracting water cycle enter extracting and separating tank 6 operate run for extracting DME/ methyl alcohol, the flow of extracting water is 70000 ~ 90000kg/h; The working pressure of depropanizing tower is set to 1.88 ~ 2.28MPaG; Adjustment depropanizing tower column bottom temperature to 95 ~ 120 DEG C; Start to inject methyl alcohol slowly, the flow of methyl alcohol can adjust flexibly, and methanol flow is 20000 ~ 450000kg/h, and regular constantly at tower top sampling detection water and methanol content, and adjusts quantity of reflux and Ta Wen gradually; DME and methyl alcohol accumulate at the bottom of depropanizing tower 1 tower, enter extracting and separating tank 6 and C4
+hydrocarbon is separated and enters methanol distillation column 7, returns in DME reactor 8 after refining, and methyl alcohol reacts raw DME, DME and enters the lighter hydrocarbons that MTP reactor generates low carbon atom number under catalyst action.
Embodiment 2
As shown in Figure 1, remove in a kind of MTP technique of the present invention, 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 successively with deethanizing column 2, propylene tower 3 and propylene product tank 5 serial communication; Discharge port at the bottom of the tower of depropanizing tower 1 successively with extracting and separating tank 6, methanol distillation column 7, DME reactor 8 and MTP reactor 9 serial communication; Described depropanizing tower 1 is also provided with methanol feeding mouth.Also be provided with overhead product on line analyzer 10 for detecting 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.Regeneration protection bed 4 is also provided with between propylene tower 3 and propylene product tank 5; the opening for feed of regeneration protection bed 4 is communicated with the discharge port of propylene tower 3; the discharge port of regeneration protection bed 4 is communicated with the opening for feed of propylene product tank 5, for absorbing DME, water and the methyl alcohol that may be mixed in propylene product.Wherein, liquid outlet at the bottom of methanol distillation column 7 tower is communicated with a fluid inlet of extracting and separating tank 6, dissolves methyl alcohol and DME for the extracting water cycle at methanol distillation column 7 end is injected 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 only be described the preferred embodiment of the present invention; not scope of the present invention is limited; under not departing from the present invention and designing the prerequisite of spirit; the various distortion that those of ordinary skill in the art make technical scheme of the present invention and improvement, all should fall in protection domain that claims of the present invention determines.
Claims (6)
1. remove in MTP technique, 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, directly inject dissolve with methanol solution DME, methane, ethane, ethene, propylene, C3 hydrocarbon are steamed from tower top, C4 in depropanizing tower
+hydrocarbon and DME/ methyl alcohol distillate and enter extracting and separating tank at the bottom of tower; In extracting and separating tank, DME/ methyl alcohol and C4
+hydrocarbon enters methanol distillation column after being separated, and the refining DME/ methyl alcohol feeding DME reactor steamed through methanol distillation column carries out cycling and reutilization.
2. method according to claim 1, is characterized in that: the quantity of reflux increasing depropanizing tower tower top, until tower top steams C4 in thing
+till hydrocarbon content maybe cannot detect lower than the Monitoring lower-cut 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, column bottom temperature 95 ~ 120 DEG C.
4. method according to claim 1; it is characterized in that: before methanol feedstock injects depropanizing tower; stablize propylene tower operation, and the regeneration protection bed of propylene tower overhead product line downstream as protector is put into operation, absorb DME, water and the methyl alcohol that may be mixed in propylene product.
5. method according to claim 1, is characterized in that: the extracting water at the bottom of methanol distillation column tower is injected 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, and constantly adjustment injects the flow of methyl alcohol, the content of first alcohol and water in regular detection overhead product.
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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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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN105439800B (en) * | 2015-12-30 | 2018-06-08 | 神华集团有限责任公司 | DME removing system and methods in MTP products |
| CN107721829B (en) * | 2016-08-12 | 2020-09-18 | 惠生工程（中国）有限公司 | Method for removing dimethyl ether from raw material flow containing propane and dimethyl ether |
| US10647623B2 (en) * | 2018-08-10 | 2020-05-12 | Uop Llc | Processes for reduced oxygenated recycle in an MTO conversion |
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| CN1795156A (en) * | 2003-04-22 | 2006-06-28 | 环球油品公司 | Selective dimethylether recovery and recycle in a methanol-to-olefin process |
| US7132580B1 (en) * | 2003-05-13 | 2006-11-07 | Uop Llc | Selective dimethylether and methanol recovery and recycle in a methanol-to-olefin process |
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| AU783766B2 (en) * | 2000-06-23 | 2005-12-01 | Jgc Corporation | Process for the preparation of lower olefins |
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| CN1795156A (en) * | 2003-04-22 | 2006-06-28 | 环球油品公司 | Selective dimethylether recovery and recycle in a methanol-to-olefin process |
| US7132580B1 (en) * | 2003-05-13 | 2006-11-07 | Uop Llc | Selective dimethylether and methanol recovery and recycle in a methanol-to-olefin process |
| CN101130484A (en) * | 2007-09-07 | 2008-02-27 | 中国寰球工程公司 | Pressure-reducing flow-reversing dual-purpose distillation method and apparatus for refining crude methanol |
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Address after: Two road 100012 Beijing city Chaoyang District high tech Industrial Park, No. 1. Patentee after: China Global Engineering Co. Ltd. Address before: Two road 100012 Beijing city Chaoyang District high tech Industrial Park, No. 1. Patentee before: China Huanqiu Engineering Co. |
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Effective date of registration: 20201204 Address after: 100120 Beijing Xicheng District six laying Kang Patentee after: CHINA NATIONAL PETROLEUM Corp. Patentee after: CHINA HUANQIU CONTRACTING & ENGINEERING Co.,Ltd. Address before: Two road 100012 Beijing city Chaoyang District high tech Industrial Park, No. 1. Patentee before: CHINA HUANQIU CONTRACTING & ENGINEERING Co.,Ltd. |