CN108191598A - The method of handoff-security ethylene unit C_3 hydrogenation reactor - Google Patents
The method of handoff-security ethylene unit C_3 hydrogenation reactor Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
- C07C5/05—Partial hydrogenation
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- C07—ORGANIC CHEMISTRY
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Abstract
The present invention relates to a kind of methods of handoff-security ethylene unit C_3 hydrogenation reactor, mainly solve the problems, such as that operation element amount is big in the prior art, security reliability is poor.The present invention is by using a kind of method of handoff-security ethylene unit C_3 hydrogenation reactor, C_3 hydrogenation reactor is subjected to normal and regeneration regime one key switching, retain interlock, without human intervention, normally dropped to 0.1 second from 60~180 seconds with regeneration regime switching time；Hydrogenated C3 fraction detaches again, obtains propylene content >=99.6mol%, propine content≤5 × 10‑6Mol, allene content≤5 × 10‑6The technical solution of the polymerization-grade propylene product of mol preferably solves the above problem, available in ethylene unit C_3 hydrogenation reactor handoff-security.
Description
Technical field
The present invention relates to a kind of methods of handoff-security ethylene unit C_3 hydrogenation reactor.
Background technology
In ethylene unit production, propine and allene that C3 fraction contains 1~5mol% need to remove, general to use
Liquid phase back end hydrogenation technology carries out hydrogenation reaction in gas, liquid, solid three-phase trickle bed reactor, is converted into propine and allene
Propylene ensures the propine of polymerization-grade propylene product and allene content≤5 × 10-6mol.It is of the prior art
A kind of systems for improving three alkynes hydrogenation selectivity of ethylene unit carbon of CN201520902811.0, disclose a kind of three alkynes of carbon and add
The system of hydrogen selectivity is increased economic efficiency with improving C_3 hydrogenation reactor selectivity；A kind of gas of CN200910259974.0
The mixed aerosol device cooling protection system of fluidized bed reactor discloses the system and is made of 12 subsystems, can effectively be protected
Equipment is protected, improves the safety of the utilization of capacity of entrained-flow reactor, support personnel and equipment；CN201510500998.6 prevents high tower
The method that ammonium nitrate fires in production nitrate-based compound fertilizer technique is granulated, is disclosed by setting overtemperature alarm interlocking protective system
To reactor into trip temperature implementing monitoring with improve production nitrate-based compound fertilizer technique safety.
CN201520902811.0 of the prior art discloses only the ethylene cracking gas in nominal situation and selects
Add the method for hydrogen and corresponding technology, do not consider the technical measures of accident conditions and regeneration regime, more without switching side accordingly
Method.CN200910259974.0 and CN201510500998.6, which is disclosed only, protects reactor and production line in nominal situation
Method and corresponding measure and nominal situation and accident conditions between the technical measures that switch.The prior art is only as a result,
Consider the defencive function under nominal situation, once hydrogenation reactor enters regeneration regime, need hydrogenation reactor from technique stream
It is switched out in journey, is transferred to manual mode, the regenerative operation of hydrogenation reactor could be completed.When hydrogenation reactor regenerates, need
The safety interlocking of hydrogenation reactor is switched to bypass, at this time hydrogenation reactor lack interlock protection or needs it is artificial general
For part valve imperative operation to "ON" or off position, operation element amount is big, it is also possible to the danger of human operational error occurs
Situation.There are the problem of security reliability is poor, operation element amount is big for the prior art as a result,.
Invention content
The technical problems to be solved by the invention are the problem of operation element amount are big, security reliability is poor in the prior art,
A kind of method of new handoff-security ethylene unit C_3 hydrogenation reactor is provided, has that operation element amount is small, security reliability
The advantages of good.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of handoff-security ethylene unit C_3 hydrogenation
The method of reactor realizes that C3 fraction carries out two kinds of the back end hydrogenation reactor nominal situation of catalytic hydrogenation reaction and regeneration regime
The one key switching of operation mode, under nominal situation operation mode, the security interlocking protection function of C_3 hydrogenation reactor is normal
Operation, once overheating problem occurs in C_3 hydrogenation reactor, is immediately switched to accident conditions, avoids C_3 hydrogenation reactor into one
Temperature runaway phenomenon occurs for step, so as to protect hydrogenation reactor process equipment completely, prevents accident；It is operated in regeneration regime
Under pattern, which enters the security interlocking protection state of regeneration regime, and the setting value for interlocking temperature is automatically changed to regenerate
The setting value of operating mode, C3 fraction stop entering the reactor, in order to prevent regeneration regime reactor feed maloperation, carbon three
Fraction input and output material valve passes through safety interlocking positive closing；In addition, during the reactor regenerative operation, still ensure that in technological process
Other C_3 hydrogenation reactor normal operations；Meanwhile the accident conditions stop sign of other C_3 hydrogenation reactors also not shadow
Ring the regenerative operation of the reactor.
In above-mentioned technical proposal, it is preferable that by the different production scale of ethylene unit, 2~4 C_3 hydrogenations is set to react
Device is required with reaching the technology.
In above-mentioned technical proposal, it is preferable that 4 C_3 hydrogenation reactors of setting：C_3 hydrogenation reactor (5) and carbon three add
Hydrogen reactor (6) and C_3 hydrogenation reactor (7) normal operation and C_3 hydrogenation reactor (8) regenerative operation；From out-of-bounds
Depropanizing tower charging (41) carry out material rectifying separation into depropanizing tower (1), tower top isolates C3 fraction material (42),
Tower reactor is isolated material (45) and is sent out out-of-bounds；Depropanizing tower (1) tower top C3 fraction material (42) is returned into depropanizing tower tower top
Tank (2) is flowed all to condense, a part of liquid phase material returns to depropanizing tower (1) tower top as depropanizing tower overhead reflux liquid (43),
Another part liquid phase material (44) is into water collector (3) to remove the moisture in material；C_3 hydrogenation reactor (5) inlet valve
Door (21) is opened, and C_3 hydrogenation reactor (5) outlet valve (25) is opened；C_3 hydrogenation reactor (6) inlet valve (22) is beaten
It opens, C_3 hydrogenation reactor (6) outlet valve (26) is opened；C_3 hydrogenation reactor (7) inlet valve (23) is opened, and carbon three adds
Hydrogen reactor (7) outlet valve (27) is opened；The C_3 hydrogenation total reactor feed (51) flowed out from water collector (3) is divided into carbon
Three hydrogenation reactors feed (52), C_3 hydrogenation reactor feed (53), and C_3 hydrogenation reactor feed (54) respectively enters carbon
Three hydrogenation reactors (5), C_3 hydrogenation reactor (6), C_3 hydrogenation reactor (7) carry out hydrogenation reaction, and propine is hydrogenated to third
Alkene, allene are also hydrogenated to propylene；Material (56) after reaction is by adding hydrogen aftercooler (9) to remove hydrogenation reaction heat, reaction
Material (57) afterwards is by adding hydrogen aftercooler (10) to remove hydrogenation reaction heat, and the material (58) after reaction is by adding hydrogen postcooling
Device (11) removes hydrogenation reaction heat；C_3 hydrogenation reactor (8) inlet valve (24) is closed, C_3 hydrogenation reactor (8) outlet
Valve (28) is closed, and C_3 hydrogenation reactor (8) carries out regenerative operation；Material (56) after hydrogenation reaction, after hydrogenation reaction
Material (57), the material (58) after hydrogenation reaction merge into C_3 hydrogenation reactor always discharge (60) send out out-of-bounds.
In above-mentioned technical proposal, ethylene unit C_3 hydrogenation reactor catalyst is using Beijing Chemical Research Institute's exploitation
BC-L-83 type catalyst, palladium Pd contents are 0.3%, 40~100m of specific surface area2/ g, carrier are aluminium oxide Al2O3；In normal work
Reaction temperature under condition operation mode is 10~60 DEG C, and preferred scope is 15~55 DEG C, ranging from more preferably 20~50 DEG C；Reaction
Pressure is 1.0~3.0MPaG, and preferred scope is 1.2~2.8MPaG, ranging from more preferably 1.4~2.6MPaG；Liquid phase air speed 20
~90h-1；Regeneration temperature under regeneration regime operation mode is 180~260 DEG C, and preferred scope is 190~250 DEG C, more preferably
Ranging from 200~240 DEG C；Regeneration pressure is 0.6~2.0MPaG, and preferred scope is 0.8~1.8MPaG, more preferably ranging from
1.0~1.6MPaG.
Using the method for handoff-security ethylene unit C_3 hydrogenation reactor of the present invention, in nominal situation and regeneration regime two
Under kind of operation mode, one button security switching is realized, not only retained original safety interlocking function, but also without manual hand manipulation, normally
Operating mode was reduced to 0.1 second with regeneration regime switching time from 60~180 seconds；Add the C3 fraction after hydrogen by later separation essence
System, obtains propylene content >=99.6mol%, propine content≤5 × 10-6Mol, allene content≤5 × 10-6The polymer grade of mol
Propylene product；The present invention improves security reliability, reduces operation element amount as a result, achieves preferable technique effect, takes
Obtained preferable technique effect.
Description of the drawings
For 4 C_3 hydrogenation reactors are set.
Fig. 1 is the process flow diagram of handoff-security C_3 hydrogenation reactor.
In Fig. 1：1 depropanizing tower, 2 depropanizing tower return tank of top of the tower, 3 water collectors, 4 operation mode one key switching facilities,
5,6,7,8 C_3 hydrogenation reactors, 9,10,11,12 hydrogenation reactor aftercoolers, 21,22,23,24 reactor inlet valves,
25,26,27,28 reactor outlet valves, the charging of 41 depropanizing towers, the discharging of 42 depropanizing tower tower tops, 43 depropanizing tower tower tops return
Flow liquid, the charging of 44 water collectors, the discharging of 45 depropanizing tower tower reactors, 51 C_3 hydrogenation total reactor feeds, 52,53,54,55 carbon three
Hydrogenation reactor is fed, and 56,57,58,59 C_3 hydrogenation reactors discharging, 60 C_3 hydrogenation reactors always discharge.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
A kind of method of handoff-security ethylene unit C_3 hydrogenation reactor, as shown in Figure 1, to set 4 C_3 hydrogenations
For reactor, when C_3 hydrogenation reactor 5 and C_3 hydrogenation reactor 6 and 7 normal operation of C_3 hydrogenation reactor and carbon
During three 8 regenerative operations of hydrogenation reactor, enter depropanizing tower 1 from depropanizing tower charging 41 out-of-bounds and carry out material rectifying point
From tower top isolates C3 fraction material 42, and tower reactor is isolated material 45 and sent out out-of-bounds.1 tower top C3 fraction object of depropanizing tower
Material 42 enters depropanizing tower return tank of top of the tower 2, and all condensation, a part of liquid phase material are returned as depropanizing tower overhead reflux liquid 43
1 tower top of depropanizing tower is returned, another part liquid phase material 44 enters water collector 3 to remove the moisture in material.C_3 hydrogenation is anti-
5 inlet valve 21 of device is answered to open, 5 outlet valve 25 of C_3 hydrogenation reactor is opened；6 inlet valve 22 of C_3 hydrogenation reactor is beaten
It opens, 6 outlet valve 26 of C_3 hydrogenation reactor is opened；7 inlet valve 23 of C_3 hydrogenation reactor is opened, C_3 hydrogenation reactor
7 outlet valves 27 are opened；The C_3 hydrogenation total reactor feed 51 flowed out from water collector 3 is divided for C_3 hydrogenation reactor feed
52, C_3 hydrogenation reactor feed 53, C_3 hydrogenation reactor feed 54 respectively enters C_3 hydrogenation reactor 5, C_3 hydrogenation
Reactor 6, C_3 hydrogenation reactor 7 carry out hydrogenation reaction, and propine is hydrogenated to propylene, and allene is also hydrogenated to propylene.After reaction
Material 56 by plus hydrogen aftercooler 9 remove hydrogenation reaction heat, material 57 after reaction by plus hydrogen aftercooler 10 remove
Hydrogenation reaction heat, the material 58 after reaction is by adding hydrogen aftercooler 11 to remove hydrogenation reaction heat.8 entrance of C_3 hydrogenation reactor
Valve 24 is closed, and 8 outlet valve 28 of C_3 hydrogenation reactor is closed, and C_3 hydrogenation reactor 8 carries out regenerative operation.Hydrogenation reaction
Material 56 afterwards, the material 57 after hydrogenation reaction, the material 58 after hydrogenation reaction merge into the always discharging 60 of C_3 hydrogenation reactor
It sends out out-of-bounds.
When C_3 hydrogenation reactor 5 and C_3 hydrogenation reactor 6 and 8 normal operation of C_3 hydrogenation reactor, carbon three adds
During 7 regenerative operation of hydrogen reactor, 5 inlet valve 21 of C_3 hydrogenation reactor is opened, and 5 outlet valve 25 of C_3 hydrogenation reactor is beaten
It opens, 6 inlet valve 22 of C_3 hydrogenation reactor is opened, and 6 outlet valve 26 of C_3 hydrogenation reactor is opened, C_3 hydrogenation reactor
7 inlet valves 23 are closed, and 7 outlet valve 27 of C_3 hydrogenation reactor is closed, and 8 inlet valve 24 of C_3 hydrogenation reactor is opened,
8 outlet valve 28 of C_3 hydrogenation reactor is opened.
When C_3 hydrogenation reactor 5 and C_3 hydrogenation reactor 7 and 8 normal operation of C_3 hydrogenation reactor, carbon three adds
During 6 regenerative operation of hydrogen reactor, 5 inlet valve 21 of C_3 hydrogenation reactor is opened, and 5 outlet valve 25 of C_3 hydrogenation reactor is beaten
It opens, 6 inlet valve 22 of C_3 hydrogenation reactor is closed, and 6 outlet valve 26 of C_3 hydrogenation reactor is closed, C_3 hydrogenation reactor
7 inlet valves 23 are opened, and 7 outlet valve 27 of C_3 hydrogenation reactor is opened, and 8 inlet valve 24 of C_3 hydrogenation reactor is opened,
8 outlet valve 28 of C_3 hydrogenation reactor is opened.
When C_3 hydrogenation reactor 6 and C_3 hydrogenation reactor 7 and 8 normal operation of C_3 hydrogenation reactor, carbon three adds
During 5 regenerative operation of hydrogen reactor, 5 inlet valve 21 of C_3 hydrogenation reactor is closed, and 5 outlet valve 25 of C_3 hydrogenation reactor closes
It closes, 6 inlet valve 22 of C_3 hydrogenation reactor is opened, and 6 outlet valve 26 of C_3 hydrogenation reactor is opened, C_3 hydrogenation reactor
7 inlet valves 23 are opened, and 7 outlet valve 27 of C_3 hydrogenation reactor is opened, and 8 inlet valve 24 of C_3 hydrogenation reactor is opened,
8 outlet valve 28 of C_3 hydrogenation reactor is opened.
By nominal situation of the present invention and two kinds of operation mode one key switching facilities 4 of regeneration regime, can realize：(1) carbon
Three hydrogenation reactors 5 and C_3 hydrogenation reactor 6 and 7 normal operation of C_3 hydrogenation reactor and C_3 hydrogenation reactor 8 are again
Raw operation, (2) C_3 hydrogenation reactor 5 and C_3 hydrogenation reactor 6 and 8 normal operation of C_3 hydrogenation reactor and carbon three plus
7 regenerative operation of hydrogen reactor, (3) C_3 hydrogenation reactor 5 and C_3 hydrogenation reactor 7 and C_3 hydrogenation reactor 8 are normal
It runs and 6 regenerative operation of C_3 hydrogenation reactor, (4) C_3 hydrogenation reactor 6 and C_3 hydrogenation reactor 7 and C_3 hydrogenation
8 normal operation of reactor and 5 regenerative operation of C_3 hydrogenation reactor, the mistake of one key switching between above-mentioned (1), (2), (3), (4)
Journey.
Using the method for handoff-security ethylene unit C_3 hydrogenation reactor of the present invention, production scale is 1,500,000 tons/year of second
Alkene device sets 4 C_3 hydrogenation reactors：C_3 hydrogenation reactor 5 and the reaction of C_3 hydrogenation reactor 6 and C_3 hydrogenation
7 normal operation of device and 8 regenerative operation of C_3 hydrogenation reactor；From out-of-bounds depropanizing tower charging 41 enter depropanizing towers 1 into
The rectifying of row material detaches, and tower top isolates C3 fraction material 42, and tower reactor is isolated material 45 and sent out out-of-bounds；1 tower of depropanizing tower
It pushes up C3 fraction material 42 and enters all condensations of depropanizing tower return tank of top of the tower 2, a part of liquid phase material is as depropanizing tower tower
It pushes up phegma 43 and returns to 1 tower top of depropanizing tower, another part liquid phase material 44 enters water collector 3 to remove the water in material
Point；5 inlet valve 21 of C_3 hydrogenation reactor is opened, and 5 outlet valve 25 of C_3 hydrogenation reactor is opened；C_3 hydrogenation reactor
6 inlet valves 22 are opened, and 6 outlet valve 26 of C_3 hydrogenation reactor is opened；7 inlet valve 23 of C_3 hydrogenation reactor is opened,
7 outlet valve 27 of C_3 hydrogenation reactor is opened；The C_3 hydrogenation total reactor feed 51 flowed out from water collector 3 is divided for carbon three
Hydrogenation reactor charging 52, it is anti-to respectively enter C_3 hydrogenation for C_3 hydrogenation reactor feed 53, C_3 hydrogenation reactor feed 54
Device 5, C_3 hydrogenation reactor 6 are answered, C_3 hydrogenation reactor 7 carries out hydrogenation reaction, and propine is hydrogenated to propylene, and allene also adds hydrogen
For propylene；Material 56 after reaction is by adding hydrogen aftercooler 9 to remove hydrogenation reaction heat, and the material 57 after reaction is after adding hydrogen
Cooler 10 removes hydrogenation reaction heat, and the material 58 after reaction is by adding hydrogen aftercooler 11 to remove hydrogenation reaction heat；Carbon three adds
8 inlet valve 24 of hydrogen reactor is closed, and 8 outlet valve 28 of C_3 hydrogenation reactor is closed, and C_3 hydrogenation reactor 8 is regenerated
Operation；Material 56 after hydrogenation reaction, the material 57 after hydrogenation reaction, it is anti-that the material 58 after hydrogenation reaction merges into C_3 hydrogenation
Device is answered always to discharge 60 submittings out-of-bounds.
5,6,7 entrance material of C_3 hydrogenation reactor forms, such as the following table 1：
1 C_3 hydrogenation reactor inlet material of table forms list
| Ingredient names | Carbon two and carbon are below two | Propine and allene | Propylene | Propane | Carbon four and more than four carbon |
| Mol% | 2.62 | 3.06 | 91.98 | 2.10 | 0.24 |
Process operation parameter is as follows：BC-L-83 types catalyst Pd contents are used as 0.3%, specific surface area 55m2/ g, carrier
For aluminium oxide Al2O3；Reaction temperature under nominal situation operation mode is 25 DEG C, reaction pressure 1.7MPaG, liquid phase air speed
35h-1；Regeneration temperature under regeneration regime operation mode is 195 DEG C, regeneration pressure 1.5MPaG.
5,6,7 outlet material of C_3 hydrogenation reactor forms, such as the following table 2：
2 C_3 hydrogenation reactor outlet material of table forms list
| Ingredient names | Carbon two and carbon are below two | Propine and allene | Propylene | Propane | Carbon four and more than four carbon |
| Mol% | 0.48 | 0.00 | 95.34 | 3.96 | 0.22 |
By nominal situation of the present invention and two kinds of operation mode one key switching facilities 4 of regeneration regime, can realize：(1) carbon
Three hydrogenation reactors 5 and C_3 hydrogenation reactor 6 and 7 normal operation of C_3 hydrogenation reactor and C_3 hydrogenation reactor 8 are again
Raw operation, (2) C_3 hydrogenation reactor 5 and C_3 hydrogenation reactor 6 and 8 normal operation of C_3 hydrogenation reactor and carbon three plus
7 regenerative operation of hydrogen reactor, (3) C_3 hydrogenation reactor 5 and C_3 hydrogenation reactor 7 and C_3 hydrogenation reactor 8 are normal
It runs and 6 regenerative operation of C_3 hydrogenation reactor, (4) C_3 hydrogenation reactor 6 and C_3 hydrogenation reactor 7 and C_3 hydrogenation
8 normal operation of reactor and 5 regenerative operation of C_3 hydrogenation reactor, the mistake of one key switching between above-mentioned (1), (2), (3), (4)
Journey.
The method for using handoff-security of the present invention as a result, nominal situation and two kinds of mutual handoff procedures of pattern of regeneration regime
In, handoff procedure spends 0.1 second time, and security reliability is good, operation element amount is small.Add the C3 fraction after hydrogen by follow-up point
From refining, propylene content >=99.6mol%, propine content≤5 × 10 are obtained-6Mol, allene content≤5 × 10-6Mol's is poly-
Close grade propylene product.
【Comparative example 1】
Prior art production scale is 1,500,000 tons/year of ethylene units, and two kinds of patterns of nominal situation and regeneration regime are mutually cut
During changing, using manual hand manipulation, handoff procedure spends 180 seconds time, and security reliability is poor, operation element amount is big.
【Embodiment 2】
Together【Embodiment 1】, only production scale be changed to 11.5 ten thousand tons/year, 2 C_3 hydrogenation reactors are set：1 normal
Operation, 1 regenerative operation.Using the method for handoff-security of the present invention, two kinds of patterns of nominal situation and regeneration regime mutually switch
In the process, handoff procedure spends 0.1 second time, and security reliability is good, operation element amount is small.After adding the warp of the C3 fraction after hydrogen
Continuous separation and purification, obtains propylene content >=99.6mol%, propine content≤5 × 10-6Mol, allene content≤5 × 10-6mol
Polymerization-grade propylene product.
【Comparative example 2】
Prior art production scale is 11.5 ten thousand tons/year of ethylene units, and two kinds of patterns of nominal situation and regeneration regime are mutual
In handoff procedure, using manual hand manipulation, handoff procedure spends 60 seconds time, and security reliability is poor, operation element amount is big.
【Embodiment 3】
Together【Embodiment 1】, only production scale be changed to 1,000,000 tons/year, 3 C_3 hydrogenation reactors are set：2 normal
Operation, 1 regenerative operation.Using the method for handoff-security of the present invention, two kinds of patterns of nominal situation and regeneration regime mutually switch
In the process, handoff procedure spends 0.1 second time, and security reliability is good, operation element amount is small.After adding the warp of the C3 fraction after hydrogen
Continuous separation and purification, obtains propylene content >=99.6mol%, propine content≤5 × 10-6Mol, allene content≤5 × 10-6mol
Polymerization-grade propylene product.
【Comparative example 3】
Prior art production scale is 1,000,000 tons/year of ethylene units, and two kinds of patterns of nominal situation and regeneration regime are mutually cut
During changing, using manual hand manipulation, handoff procedure spends 120 seconds time, and security reliability is poor, operation element amount is big.
【Embodiment 4】
Together【Embodiment 1】, only process operation parameter change, process operation parameter are as follows：Using BC-L-83 type catalyst
Pd contents are 0.3%, specific surface area 40m2/ g, carrier are aluminium oxide Al2O3；Reaction temperature under nominal situation operation mode
It is 10 DEG C, reaction pressure 1.0MPaG, liquid phase air speed 20h-1；Regeneration temperature under regeneration regime operation mode is 180 DEG C,
Regeneration pressure is 0.6MPaG.
The method for using handoff-security of the present invention as a result, nominal situation and two kinds of mutual handoff procedures of pattern of regeneration regime
In, handoff procedure spends 0.1 second time, and security reliability is good, operation element amount is small.Add the C3 fraction after hydrogen by follow-up point
From refining, propylene content >=99.6mol%, propine content≤5 × 10 are obtained-6Mol, allene content≤5 × 10-6Mol's is poly-
Close grade propylene product.
【Embodiment 5】
Together【Embodiment 1】, only process operation parameter change, process operation parameter are as follows：Using BC-L-83 type catalyst
Pd contents are 0.3%, specific surface area 100m2/ g, carrier are aluminium oxide Al2O3；Reaction temperature under nominal situation operation mode
It is 60 DEG C, reaction pressure 3.0MPaG, liquid phase air speed 90h-1；Regeneration temperature under regeneration regime operation mode is 260 DEG C,
Regeneration pressure is 2.0MPaG.
The method for using handoff-security of the present invention as a result, nominal situation and two kinds of mutual handoff procedures of pattern of regeneration regime
In, handoff procedure spends 0.1 second time, and security reliability is good, operation element amount is small.Add the C3 fraction after hydrogen by follow-up point
From refining, propylene content >=99.6mol%, propine content≤5 × 10 are obtained-6Mol, allene content≤5 × 10-6Mol's is poly-
Close grade propylene product.
Claims (8)
1. a kind of method of handoff-security ethylene unit C_3 hydrogenation reactor realizes that C3 fraction carries out catalytic hydrogenation reaction
The one key switching of back end hydrogenation reactor nominal situation and two kinds of operation modes of regeneration regime, under nominal situation operation mode, carbon
The security interlocking protection function normal operation of three hydrogenation reactors, once overheating problem occurs in C_3 hydrogenation reactor, cuts immediately
Accident conditions are changed to, avoid C_3 hydrogenation reactor that temperature runaway phenomenon further occurs, so as to protect hydrogenation reactor completely
Process equipment prevents accident；Under regeneration regime operation mode, which enters the security interlocking protection of regeneration regime
State, the setting value for interlocking temperature are automatically changed to the setting value of regeneration regime, and C3 fraction stops entering the reactor, in order to
The regeneration regime reactor feed maloperation is prevented, C3 fraction input and output material valve passes through safety interlocking positive closing；It in addition, should
During reactor regenerative operation, other C_3 hydrogenation reactor normal operations in technological process are still ensured that；Meanwhile other carbon three
The accident conditions stop sign of hydrogenation reactor nor affects on the regenerative operation of the reactor.
2. the method for handoff-security ethylene unit C_3 hydrogenation reactor according to claim 1, it is characterised in that by ethylene
The different production scale of device sets 2~4 C_3 hydrogenation reactors.
3. the method for handoff-security ethylene unit C_3 hydrogenation reactor according to claim 1, it is characterised in that setting 4
C_3 hydrogenation reactor：C_3 hydrogenation reactor (5) and C_3 hydrogenation reactor (6) and C_3 hydrogenation reactor (7) are normal
It runs and C_3 hydrogenation reactor (8) regenerative operation；It is carried out from depropanizing tower charging (41) out-of-bounds into depropanizing tower (1)
Material rectifying detaches, and tower top isolates C3 fraction material (42), and tower reactor is isolated material (45) and sent out out-of-bounds；Depropanizing tower
(1) tower top C3 fraction material (42) is all condensed into depropanizing tower return tank of top of the tower (2), and a part of liquid phase material is as de-
Propane column overhead phegma (43) return depropanizing tower (1) tower top, another part liquid phase material (44) into water collector (3) with
Remove the moisture in material；C_3 hydrogenation reactor (5) inlet valve (21) is opened, C_3 hydrogenation reactor (5) outlet valve
(25) it opens；C_3 hydrogenation reactor (6) inlet valve (22) is opened, and C_3 hydrogenation reactor (6) outlet valve (26) is opened；
C_3 hydrogenation reactor (7) inlet valve (23) is opened, and C_3 hydrogenation reactor (7) outlet valve (27) is opened；Assemble from water
The C_3 hydrogenation total reactor feed (51) of device (3) outflow is divided into C_3 hydrogenation reactor feed (52), C_3 hydrogenation reactor
It feeding (53), C_3 hydrogenation reactor feed (54) respectively enters C_3 hydrogenation reactor (5), C_3 hydrogenation reactor (6),
C_3 hydrogenation reactor (7) carries out hydrogenation reaction, and propine is hydrogenated to propylene, and allene is also hydrogenated to propylene；Material after reaction
(56) by hydrogen aftercooler (9) is added to remove hydrogenation reaction heat, the material (57) after reaction is by adding hydrogen aftercooler (10) to move
Hydrogenation reaction heat is walked, the material (58) after reaction is by adding hydrogen aftercooler (11) to remove hydrogenation reaction heat；C_3 hydrogenation reacts
Device (8) inlet valve (24) is closed, and C_3 hydrogenation reactor (8) outlet valve (28) is closed, and C_3 hydrogenation reactor (8) carries out
Regenerative operation；Material (56) after hydrogenation reaction, the material (57) after hydrogenation reaction, the material (58) after hydrogenation reaction are merged into
C_3 hydrogenation reactor always discharges (60) submitting out-of-bounds.
4. the method for handoff-security ethylene unit C_3 hydrogenation reactor according to claim 1, it is characterised in that ethylene fills
The BC-L-83 type catalyst that C_3 hydrogenation reactor catalyst uses Beijing Chemical Research Institute's exploitation is put, palladium Pd contents are
0.3%, 40~100m of specific surface area2/ g, carrier are aluminium oxide Al2O3。
5. the method for handoff-security ethylene unit C_3 hydrogenation reactor according to claim 1, it is characterised in that normal
Reaction temperature under operating mode operation mode is 10~60 DEG C, and reaction pressure is 1.0~3.0MPaG, 20~90h of liquid phase air speed-1。
6. the method for handoff-security ethylene unit C_3 hydrogenation reactor according to claim 5, it is characterised in that normal
Reaction temperature under operating mode operation mode is 20~50 DEG C；1.4~2.6MPaG of reaction pressure.
7. the method for handoff-security ethylene unit C_3 hydrogenation reactor according to claim 1, it is characterised in that regenerating
Regeneration temperature under operating mode operation mode is 180~260 DEG C, and regeneration pressure is 0.6~2.0MPaG.
8. the method for handoff-security ethylene unit C_3 hydrogenation reactor according to claim 7, it is characterised in that regenerating
Regeneration temperature under operating mode operation mode is 200~240 DEG C；Regeneration pressure is 1.0~1.6MPaG.
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