CN1023445C - Catalytic reaction method with variable total height of bed layer and apparatus therefor - Google Patents
Catalytic reaction method with variable total height of bed layer and apparatus therefor Download PDFInfo
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- CN1023445C CN1023445C CN 89101272 CN89101272A CN1023445C CN 1023445 C CN1023445 C CN 1023445C CN 89101272 CN89101272 CN 89101272 CN 89101272 A CN89101272 A CN 89101272A CN 1023445 C CN1023445 C CN 1023445C
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- bed
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Abstract
The present invention relates to a catalytic reaction device with variable bed overall height, which has the advantages of flexible operation and simple structure. The present invention is provided with a fixed bed reactor, and the requirement of changing the catalytic dosage is achieved by adopting a method for adding gradually the bed height of the catalytic reactor. Compared with the general fixed bed reactor, the present invention has the advantages of long operation cycle and high average selectivity in a full operation cycle.
Description
The invention belongs to reaction engineering part in the field of chemical engineering.
The catalyst of any catalytic reaction its activity in a service cycle all progressively descends, and difference only is the active speed difference that descends, thereby the reactor types difference that adopts.Be applicable to the reaction that inactivation is exceedingly fast as fluidized-bed reactor, fixed bed reactors are applicable to the reactor that deactivation rate is slower, but any reactor no matter, its catalyst amount all is changeless in running, this is at patent US.4313908, US4330505, US4233268, all be described among the clear 59-126407 of CN86103973 and Te Kai, wherein the fixed bed reactors described in US4313903 and the US4330505 also can change the bed total height, this fixed bed reactors are that auxiliary bed is set on main bed, carry out in the catalytic reaction process when auxiliary bed silts up, gas phase and/or the liquid phase material of participating in reaction enter main bed by the bypass that is arranged in the reactor, this moment, total bed height of reactor reduced, but but prolong operation cycle by above-mentioned prior art as can be known, had not also had employing to come the catalytic reaction method of prolong operation cycle to increase the reactor beds layer height.
The objective of the invention is to solve weak point among the above-mentioned prior art, the method for taking progressively to increase the catalytic reactor bed height realizes increasing catalytic amount to reach prolong operation cycle, improves the purpose of reaction selectivity simultaneously.
Realize that device of the present invention is variable bed total height catalyst reaction device, sees shown in the accompanying drawing one.In fixed bed catalytic reactor R, A is set
(1-n)And B
(1-n)Beds, A and B can be the single hop bed and also can be two sections or multistage bed, and A and B beds can be arranged in the same reactor, also can be arranged in two reactors or a plurality of reactor, and each reactor is equipped with feed(raw material)inlet valve V
FiWith suction line 3, reactor bottom is provided with reactant discharge valve V
EiWith outlet line 4, each reactor also is provided with the reactant discharge valve V of flow direction reactor in succession
Si, then V needn't be set if this reactor fixedly is in last reactor location of the flow direction
SiValve.At this device operation initial stage, when catalyst activity is high only bed Ai come into operation, participate in the raw material gas phase of reaction and/or liquid phase by pipeline 1,2, feed(raw material)inlet valve V
FiEnter reactor with pipeline 3, raw material reacts at reaction bed Ai, when the catalysqt deactivation on the Ai bed does not promptly reach the conversion ratio of regulation, can regulate the inlet amount that enters bed Ai, off-response device outlet valve V
E1, breakdown reactor bypass feed(raw material)inlet valve V
Si, raw material enters B
1Bed, at the catalyst activity height, reactant passes through B when reaching the conversion ratio of regulation
1Bed is through outlet valve V
E2Leave reactor.When reacting again less than the regulation conversion ratio, can valve-off V
B2, breakdown bypass valve V
S2Make the intact material of unreacted enter next beds, also can make reactor enter the catalyst regeneration program by terminating operation.The number of B bed determines according to response characteristic and technological requirement.
The size of effect of the present invention is relevant with response characteristic, more is the reaction speed height that polyphone is paid reaction, and during the serious inactivation of bed bottom catalyst, effect of the present invention more demonstrates superiority.Adopt the method that increases the catalyst bed layer height to solve selection of catalysts and the contradiction between the operation cycle, be that catalytic reaction initial stage catalyst activity height then adopts low bed height, can shorten polyphone and pay the reaction time of reaction, when reaction later stage conversion ratio descends, adopt the method that increases the catalyst bed layer height to be implemented in and reach the average selectivity height in the prolong operation cycle and keep stable conversion ratio.When general fixed bed reactors total height equated situation shown in the total height of variable bed height reactor and the accompanying drawing two, then variable bed height reaction unit can the prolong operation cycle twice.The present invention is applicable to catalytic reaction process, is specially adapted to benzene alkylation, the alkylation of toluene course of reaction.
Accompanying drawing one explanation:
1 and 2 enter the feed line of catalyst reaction device.
3 enter the material pipeline of catalytic reactor.
The pipeline of 4 output-response products.
V
1Enter the material valve of catalytic reactor.
V
2The valve of connecting pipe is also referred to as bypass valve between two beds (or reactor).
V
EReactor discharging valve.
The beds that the A reaction unit just comes into operation when driving.
The beds that B comes into operation behind bed A inactivation.
The variable bed total height of R catalytic reactor.
Accompanying drawing two explanations:
11 and 12 enter the feed line of catalyst reaction device.
13 reacting product outlet pipelines.
The conventional fixed bed reactors of E.
A
1～A
4Beds.
Embodiment
Benzene and ethylene reaction generate ethylo benzene, and the key reaction process is as follows:
Ethylbenzene is the purpose product of reaction, and diethylbenzene can generate ethylbenzene with the benzene reaction, but Returning reactor enters the mouth after separating.Toluene and dimethylbenzene are that accessory substance plays reduction and optionally acts on.Ethylbenzene, ethene, benzene, diethylbenzene, toluene all can make catalysqt deactivation, are different but make the rate constant of catalysqt deactivation, and its rule is an ethene ethylbenzene benzene.Benzene alkene ratio in the raw material charging is 15 o'clock, and catalytic reactor middle and upper part bed inactivation is mainly caused by ethene, mainly is aromatic hydrocarbons and the bottom causes catalysqt deactivation.Various deactivation stacks, it is rapid to make beds present the upper strata inactivation, and lower floor's inactivation is slower, the deactivation feature that the forward position of serious inactivation layer progressively moves down.Adopt and change catalyst amount, the change that is bed height comes prolong operation cycle, the fixed-bed reactor operation cycle shown in figure two is 35 days, adopt identical air speed to select the variable bed total height catalyst reaction device shown in the figure one for use, initial reaction stage is used four sections beds, works as catalyst activity reduction, in the time of can not reaching the conversion ratio of regulation, enable the 5th section bed, catalyst is enabled the 6th section bed during inactivation again can make the operation cycle reach 70 days.
Claims (2)
1, a kind of catalytic reaction method, it is characterized in that catalyst amount progressively increases in the operation cycle: only pass through beds A at the initial reaction stage reaction mass, when the catalyst activity reduction of bed A did not reach the conversion ratio of regulation, reaction mass entered catalytic bed B
1, make to reach behind the regulation conversion ratio and discharge again, if B
1The bed catalyst can be restarted next section bed B when inactivation does not reach the conversion ratio of regulation again
2, the height that so progressively increases bed B carries out the regeneration of catalyst when last bed comes into operation and do not reach the conversion ratio of regulation.
2, a kind of catalyst reaction device that catalyst amount was progressively increased in the operation cycle is characterized in that bed height is variable, and beds A and B can be the single hop bed, also can be the multistage bed; A and B beds can be arranged in the same reactor, also can be arranged in two reactors or a plurality of reactor, and the number of B bed determines according to response characteristic and technological requirement.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89101272 CN1023445C (en) | 1989-03-15 | 1989-03-15 | Catalytic reaction method with variable total height of bed layer and apparatus therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89101272 CN1023445C (en) | 1989-03-15 | 1989-03-15 | Catalytic reaction method with variable total height of bed layer and apparatus therefor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1040516A CN1040516A (en) | 1990-03-21 |
| CN1023445C true CN1023445C (en) | 1994-01-12 |
Family
ID=4854206
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 89101272 Expired - Lifetime CN1023445C (en) | 1989-03-15 | 1989-03-15 | Catalytic reaction method with variable total height of bed layer and apparatus therefor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1023445C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1078490C (en) * | 1996-08-02 | 2002-01-30 | 中国石油化工总公司 | Fixed bed catalytic reaction method of multistage series step-by-step change and its device |
| CN103781540A (en) * | 2011-06-16 | 2014-05-07 | 赫多特普索化工设备公司 | Method for carrying out exothermic catalytic reactions and a reactor for use in the method |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102005016369A1 (en) * | 2005-04-09 | 2006-10-12 | Degussa Ag | Process for the continuous production of methyl mercaptan |
| CN101147852B (en) * | 2006-09-20 | 2010-09-01 | 中国石油化工股份有限公司 | Multistage insulation fixed bed reactor |
| CN111574369B (en) * | 2020-06-08 | 2024-05-17 | 北京旭阳科技有限公司 | Method for preparing methyl methacrylate by condensing methyl propionate and formaldehyde aldol and multistage reaction system |
-
1989
- 1989-03-15 CN CN 89101272 patent/CN1023445C/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1078490C (en) * | 1996-08-02 | 2002-01-30 | 中国石油化工总公司 | Fixed bed catalytic reaction method of multistage series step-by-step change and its device |
| CN103781540A (en) * | 2011-06-16 | 2014-05-07 | 赫多特普索化工设备公司 | Method for carrying out exothermic catalytic reactions and a reactor for use in the method |
| CN103781540B (en) * | 2011-06-16 | 2015-12-23 | 赫多特普索化工设备公司 | For the method that performs exothermic catalytic reaction and the reactor used in the method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1040516A (en) | 1990-03-21 |
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Owner name: CHINA PETROCHEMICAL CORPORATION Free format text: FORMER OWNER: CHINA PETRO-CHEMICAL CORP. |
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| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20021220 Co-patentee after: China Petro-Chemical Corp. Patentee after: China Petrochemical Group Corp. Co-patentee before: China Petro-Chemical Corp. Patentee before: China Petrochemical Corporation |
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| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |