CN101811921A - Continuous process for preparing hydrocarbon products through methanol transformation without standby reactor - Google Patents
Continuous process for preparing hydrocarbon products through methanol transformation without standby reactor Download PDFInfo
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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
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Abstract
The invention discloses a continuous process for preparing hydrocarbon products through methanol transformation without standby reactor. Two groups of reactors are arranged; the first group reactor works first, when a catalyst in the first group of reactor reaches metaphase of lifetime one way, the second group of reactor is started, so that the two groups of reactors are in the simultaneous working state and respectively bear 50 percent of reaction load; when the catalyst in the first group of reactor reaches last phase of the lifetime one way, a catalyst in the second group of reactor is positioned in the metaphase of lifetime one way, and at the moment, the total 100 percent of reaction load is transferred to the second group of reactor and the catalyst in the first group of reactor is regenerated; after the catalyst in the first group of reactor is regenerated, the first group of reactor works, and the two groups of reactors respectively bear 50 percent of reaction load; when the catalyst in the second group of reactor reaches the last phase of the lifetime one way, the catalyst in the first group of reactor is positioned in the metaphase of the lifetime one way, and at the moment, the total 100 percent of reaction load is transferred to the first group of reactor and the catalyst in the second group of reactor is regenerated; the process is repeated so as to realize reaction process continuity under the condition of no standby reactor. The continuous process has the advantages of not needing arranging the standby reactor, simplifying process flow, reducing equipment investment and improving system operation stability and reliability.
Description
Technical field
The invention belongs to a kind of continuous processing of preparing hydrocarbon products by methanol conversion, relate in particular to a kind of continuous processing of preparing hydrocarbon products through methanol transformation without standby reactor.
Background technology
Preparing hydrocarbon products by methanol conversion is the important chemical reaction of a class, as methanol conversion system gasoline (the MTG technology of Exxon-Mobil company, Shanxi Inst. of Coal Chemistry, Chinese Academy of Sciences, match ancient cooking vessel engineering corporation, the fixed bed adiabatic reactor single stage method methanol conversion technique for preparing gasoline of Yunnan Coal Chemical Industry group cooperative development), preparing propylene by methanol transformation (the MTP technology of Lurgi company, the FMTP technology of Tsing-Hua University), methanol conversion system alkene (the MTO technology of Uop Inc., the DMTO technology of the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences), and methanol conversion for preparing arene (the MTA technology of Shanxi Inst. of Coal Chemistry, Chinese Academy of Sciences) etc., all belong to this type of reaction.
It is catalyzer that the molecular sieve with acidic surface is mostly adopted in the reaction of preparing hydrocarbon products by methanol conversion, owing to the catalyst surface carbon distribution causes the final inactivation of catalyzer, for proceeding reaction, needs regularly catalyzer to be carried out coke burning regeneration in reaction process.
In order to realize the continuity of industrial operation, these technologies are all by being provided with many reactors, wherein at least one reactor is as standby reactor, when other reactors react, standby reactor is regenerated, be in stand-by state after regeneration is finished, wait for and drop into reaction when next reactor need be regenerated.
Realize that by standby reactor is set the serialization of preparing hydrocarbon products by methanol conversion process is a successful method, still, there is following open defect in this method:
1. because standby reactor is in reproduced state or stand-by state all the time, can not bring into play its production capacity, cause the waste of equipment capacity, increase facility investment;
2. all reactors that comprise online reactor and standby reactor all need to be provided with separately catalyst regeneration process control and topworks, and the investment of control section increases automatically;
3. reactor is by platform regeneration, and the control of regeneration system rapidly and topworks's complex operation have reduced the equipment reliability of operation.
Summary of the invention
The problems referred to above at the preparing hydrocarbon products by methanol conversion process exists the purpose of this invention is to provide a kind of continuous processing that does not have the preparing hydrocarbon products by methanol conversion of standby reactor.
Above-mentioned purpose of the present invention realizes by the following method: two bank of reactor are set in the technical process of preparing hydrocarbon products by methanol conversion, open two bank of reactor respectively, when the catalyzer in the bank of reactor wherein reaches the one way end of life, catalyzer in another bank of reactor is in the mid-term in one way life-span just, this moment with the total overall reaction load transfer to the reactor that is in catalyzer one way middle of life, the catalyzer that catalyzer is in the reactor of one way end of life is regenerated simultaneously, after regeneration is finished, open immediately, and make two bank of reactor bear 50% reaction load separately.So repeatedly, be implemented in reaction process serialization under the no standby reactor condition.
Continuous processing of the present invention specifically comprises the steps:
Two bank of reactor are set in the technical process, first bank of reactor is at first devoted oneself to work, when the catalyzer in first bank of reactor reaches the one way middle of life, open second bank of reactor, make two bank of reactor be in the state of working simultaneously, and bear 50% reaction load separately, when the catalyzer of first bank of reactor reaches the one way end of life, catalyzer in second bank of reactor is in the mid-term in one way life-span, react load transfers on second bank of reactor with whole 100% this moment, and the catalyzer in first bank of reactor regenerated, devote oneself to work immediately after catalyst regeneration in first bank of reactor is finished, two bank of reactor are respectively born 50% of reaction load.When the second bank of reactor catalyzer reaches the latter stage in one way life-span, catalyzer in first bank of reactor is in the mid-term in one way life-span, at this moment, react load transfers to first bank of reactor with whole 100%, and the catalyzer in second bank of reactor regenerated, so repeatedly, be implemented in reaction process serialization under the no standby reactor condition.
Aforesaid two bank of reactor have quantity and equate, the reactor that type of reactor is identical, and according to production-scale needs, the quantity of every bank of reactor is between 1～30.But the type of reactor fixed-bed reactor, paste state bed reactor etc.
Aforesaid catalyzer is can be with the catalyzer of preparing hydrocarbon products by methanol conversion.The one way life-span of the catalyzer that is adopted is between 4～100 days.
The present invention compared with prior art has following advantage:
The continuous processing of preparing hydrocarbon products through methanol transformation without standby reactor provided by the invention compared with the prior art, one of advantage is, owing to need not to be provided with standby reactor, reduced the quantity of reactor, simplified technical process, reduced facility investment.
The continuous processing of preparing hydrocarbon products through methanol transformation without standby reactor provided by the invention compared with the prior art, another advantage is that catalyst regeneration system obtains simplifying, need not every control and topworks that reactor disposes regenerative process respectively, but reactor is divided into two groups, only dispose the control and the topworks of two groups of regenerative processes, make automatic control section simplify, reduced the investment of automatic control section.
The continuous processing of preparing hydrocarbon products through methanol transformation without standby reactor provided by the invention compared with the prior art, the 3rd advantage is the catalyst regeneration process simplified control, only between two bank of reactor, switch regeneration, improved system operation stability and reliability.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
As shown in the figure: the 1st, the methyl alcohol storage tank, the 2nd, methyl alcohol is through feedstock pump, and the 3rd, interchanger, 4, the 5th, the reacting material inlet valve, 6 is first bank of reactor, 7 is second bank of reactor, 8, the 9th, reacting material outlet valve, the 10th, pipeline, the 11,12,13, the 14th, the valve of regeneration system rapidly.
Embodiment
Technology provided by the invention can further describe as follows in conjunction with process flow diagram provided by the invention.
Embodiment 1 is an example with fixed bed adiabatic reactor single stage method methanol conversion system gasoline process, adopts the technical process of accompanying drawing.The quantity of first bank of reactor 6 and second bank of reactor 7 is 2, filling methanol conversion system gasoline catalyzing agent (ZSM-5 molecular sieve catalyst) 100kg in every reactor.Reaction pressure is 1.6MPa, and the temperature in of each reactor is 320 ℃, and temperature out is 410 ℃.Concrete implementation step is as follows.
1. open first bank of reactor
Shown in process flow sheet, when going into operation for the first time, open first bank of reactor (6) reacting material inlet valve (4), reacting material outlet valve (8), close reacting material inlet valve (5), the reacting material outlet valve (9) of second bank of reactor (7), close valve (11), (12), (13), (14) of regeneration system rapidly.Methyl alcohol flow from material benzenemethanol storage tank (1) is 200kg/h, and the methanol quality air speed is 1.0h
-1Methyl alcohol is squeezed into through feedstock pump (2) and is carried out the heat exchange intensification in the interchanger (3), after reaching the reactor inlet temperatures requirement, enter reactor (6) through first bank of reactor (6) reacting material inlet valve (4), under the effect of catalyzer, methanol conversion is the mixture of hydrocarbon product and water, through first bank of reactor (6) reacting material outlet valve (8) and pipeline (10), leave reactive system.
Second bank of reactor this moment (7) is in treats stream state, and the reactant load of first bank of reactor (6) is 50% of whole loads under the normal production conditions.
2. open second bank of reactor
When first bank of reactor (6) is worked mid-term (the 11st day) to the catalyzer one way life-span, open the material inlet valve (5) and the material outlet valve (9) of second bank of reactor (7), make reaction mass simultaneously by first bank of reactor (6) and second bank of reactor (7), and gradually the methyl alcohol flow is increased to 400kg/h, reaction this moment load reaches 100%, and the mass space velocity of methyl alcohol is 1.0h
-1First bank of reactor (6) and second bank of reactor (7) are born 50% reaction load respectively.
3. the first bank of reactor catalyst regeneration
When the catalyzer in first bank of reactor (6) arrives one way end of life (the 22nd day), close material import and export valve (4), (8) of first bank of reactor (6), make the total overall reaction material enter second bank of reactor (7), whole reaction load transfers is on second bank of reactor (7), at this moment, have only second bank of reactor (7) in running order, second bank of reactor (7) is born 100% reaction load.This moment, the mass space velocity of methyl alcohol was 2.0h with respect to the catalyzer in second bank of reactor
-1
Open valve (11), (13) of the regeneration system rapidly of first bank of reactor (6), make regeneration gas pass through first bank of reactor (6), the catalyzer in the reactor enters reproducer.
After catalyst regeneration in first bank of reactor (6) is finished, close valve (11), (13) of first bank of reactor (6) regeneration system rapidly, open terminal valve (4), (8) of the reaction mass of first bank of reactor (6), first bank of reactor is devoted oneself to work.This moment, two bank of reactor were in the state of working simultaneously, and total overall reaction is loaded evenly distribute on two bank of reactor, and every bank of reactor is born 50% reaction load.At this moment, with respect to the catalyzer in first bank of reactor and second bank of reactor, the mass space velocity of methyl alcohol is 1.0h
-1
4. the second bank of reactor catalyst regeneration
When the catalyzer in first bank of reactor (6) enters the mid-term (the 33rd day) in one way life-span, catalyzer arrives one way end of life (catalyzer in second bank of reactor has moved 22 days at this moment) in second bank of reactor (7), at this moment, close the terminal valve (5) of second bank of reactor (7) reaction mass, (9), with the total overall reaction load transfer to first bank of reactor (6), at this moment, have only first bank of reactor (6) in running order, first bank of reactor (6) is born 100% reaction load, this moment, the mass space velocity of methyl alcohol was 2.0h with respect to the catalyzer in first bank of reactor
-1
Open valve (12), (14) of second bank of reactor (7) regeneration system rapidly, the catalyzer in second bank of reactor (7) enters reproducer.
After catalyst regeneration in second bank of reactor (7) is finished, close valve (12), (14) of second bank of reactor (7) regeneration system rapidly, open terminal valve (5), (9) of the reaction mass of second bank of reactor (7), second bank of reactor (7) is devoted oneself to work.This moment, two bank of reactor were in the state of working simultaneously, and total overall reaction is loaded evenly distribute on two bank of reactor, and every bank of reactor is born 50% reaction load.At this moment, with respect to the catalyzer in first bank of reactor and second bank of reactor, the mass space velocity of methyl alcohol is 1.0h
-1
5. repeating step
When the catalyzer in second bank of reactor (7) entered the one way middle of life, the catalyzer in first bank of reactor (6) entered the latter stage in one way life-span once more, and at this moment, repeating step 3 is regenerated to the catalyzer in first bank of reactor (6).
Equally, when the catalyzer in second bank of reactor (7) arrived the latter stage in one way life-span, repetitive operation step (4) was regenerated to the catalyzer in second bank of reactor (7).
The operation of repeating step 3, step 4 can be implemented under the condition of no standby reactor the serialization of realization response process.
It is example that embodiment 2 produces the LPG reaction with methanol conversion.Adopt technical process shown in the drawings.Wherein the quantity of first bank of reactor 6 and second bank of reactor 7 is 4, loads the ZSM-5 molecular sieve catalyst 50kg that methanol conversion is produced LPG in every reactor, and the catalyst loading total amount is 400kg.The methyl alcohol flow is 800kg/h, and system pressure is 1.0MPa, and the temperature in of each reactor is 380 ℃, and the temperature out of each reactor is 510 ℃.Under the situation that reactor 6 and reactor 7 are worked simultaneously, the methanol quality air speed is 2.0h
-1, when wherein one group of catalyzer was in reproduced state, for the catalyzer in the work, the methanol quality air speed was 4.0h
-1Concrete implementation step is with embodiment 1.
Claims (5)
1. the continuous processing of a preparing hydrocarbon products through methanol transformation without standby reactor is characterized in that comprising the steps:
Two bank of reactor are set, first bank of reactor is at first devoted oneself to work, when the catalyzer in first bank of reactor reaches the one way middle of life, open second bank of reactor, make two bank of reactor be in the state of working simultaneously, and bear 50% reaction load separately, when the catalyzer of first bank of reactor reaches the one way end of life, catalyzer in second bank of reactor is in the mid-term in one way life-span, react load transfers on second bank of reactor with whole 100% this moment, and the catalyzer in first bank of reactor regenerated, after finishing, the catalyst regeneration in first bank of reactor devotes oneself to work immediately, and two bank of reactor are respectively born 50% of reaction load.When the second bank of reactor catalyzer reaches the latter stage in one way life-span, catalyzer in first bank of reactor is in the mid-term in one way life-span, at this moment, react load transfers to first bank of reactor with whole 100%, and the catalyzer in second bank of reactor regenerated, so repeatedly, be implemented in reaction process serialization under the no standby reactor condition.
2. the continuous processing of a kind of preparing hydrocarbon products through methanol transformation without standby reactor as claimed in claim 1 is characterized in that described two bank of reactor have quantity and equate, the reactor that type of reactor is identical, and the quantity of every bank of reactor is between 1～30.
3. the continuous processing of a kind of preparing hydrocarbon products through methanol transformation without standby reactor as claimed in claim 2 is characterized in that described type of reactor is fixed-bed reactor or paste state bed reactor.
4. the continuous processing of a kind of preparing hydrocarbon products through methanol transformation without standby reactor as claimed in claim 1 is characterized in that described catalyzer is the catalyzer with preparing hydrocarbon products by methanol conversion.
5. the continuous processing of a kind of preparing hydrocarbon products through methanol transformation without standby reactor as claimed in claim 4, the one way life-span that it is characterized in that described catalyzer is between 4～100 days.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104140839A (en) * | 2014-07-25 | 2014-11-12 | 山西沸石科技有限公司 | Continuous reaction and regeneration technology used for conversion of methanol to gasoline through stationary bed adiabatic reactors |
| CN107694507A (en) * | 2017-10-20 | 2018-02-16 | 中石化上海工程有限公司 | The method of automatic switchover tandem reactor pattern |
| CN107721799A (en) * | 2017-10-20 | 2018-02-23 | 中石化上海工程有限公司 | The method that parallel reactor pattern automatically switches |
| CN108191598A (en) * | 2018-01-04 | 2018-06-22 | 中石化上海工程有限公司 | The method of handoff-security ethylene unit C_3 hydrogenation reactor |
| CN108191597A (en) * | 2018-01-04 | 2018-06-22 | 中石化上海工程有限公司 | The method of ethylene unit Acetylene converter handoff-security |
| CN108329188A (en) * | 2018-01-04 | 2018-07-27 | 中石化上海工程有限公司 | The efficiently method of switching methanol-to-olefins device hydrogenation reactor |
-
2010
- 2010-04-01 CN CN2010101389733A patent/CN101811921B/en active Active
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104140839A (en) * | 2014-07-25 | 2014-11-12 | 山西沸石科技有限公司 | Continuous reaction and regeneration technology used for conversion of methanol to gasoline through stationary bed adiabatic reactors |
| CN104140839B (en) * | 2014-07-25 | 2015-09-16 | 山西沸石科技有限公司 | A kind of fixed bed adiabatic reactor methanol conversion gasoline successive reaction and reclaiming process |
| CN107694507A (en) * | 2017-10-20 | 2018-02-16 | 中石化上海工程有限公司 | The method of automatic switchover tandem reactor pattern |
| CN107721799A (en) * | 2017-10-20 | 2018-02-23 | 中石化上海工程有限公司 | The method that parallel reactor pattern automatically switches |
| CN107694507B (en) * | 2017-10-20 | 2019-11-22 | 中石化上海工程有限公司 | Automatically switch the method for tandem reactor mode |
| CN108191598A (en) * | 2018-01-04 | 2018-06-22 | 中石化上海工程有限公司 | The method of handoff-security ethylene unit C_3 hydrogenation reactor |
| CN108191597A (en) * | 2018-01-04 | 2018-06-22 | 中石化上海工程有限公司 | The method of ethylene unit Acetylene converter handoff-security |
| CN108329188A (en) * | 2018-01-04 | 2018-07-27 | 中石化上海工程有限公司 | The efficiently method of switching methanol-to-olefins device hydrogenation reactor |
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| CN101811921B (en) | 2012-11-14 |
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