CN108018073A - A kind of improved method of continuous reformer reactor displacement gas flow - Google Patents
A kind of improved method of continuous reformer reactor displacement gas flow Download PDFInfo
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- CN108018073A CN108018073A CN201610934828.3A CN201610934828A CN108018073A CN 108018073 A CN108018073 A CN 108018073A CN 201610934828 A CN201610934828 A CN 201610934828A CN 108018073 A CN108018073 A CN 108018073A
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- reactor
- gas
- catalyst
- displacement gas
- hydrocarbon
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G59/00—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha
- C10G59/02—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha plural serial stages only
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses petroleum refining and the improved method of the continuous reformer reactor displacement gas flow of chemical field, displacement gas uses the less source of the gas hydrogen of hydrocarbon-containifirst material instead by recycle hydrogen, it is bad to solve the recycle hydrogen band more purging effect of hydrocarbon, cause catalyst strips oil to influence lifting and conveying；The operation conditions of reclaimable catalyst chlorine absorber portion or chlorine tourie aggravates and causes the technical problem such as non-methane hydrocarbon discharge beyond standards in regeneration vent gas with hydrocarbon.
Description
Technical field
The invention belongs to technical field of petrochemical industry, and in particular to a kind of continuous reformer reactor displacement gas flow
Improved method.
Background technology
In CONTINUOUS REFORMER in the prior art, using reforming cycle hydrogen（Circulating air）Catalyst portion big absolutely is blown away as displacement gas
Divide oil gas, so that catalyst is lifted and is conveyed, but because reforming cycle hydrogen hydrocarbon-containifirst material is more, corresponding catalyst is continuous
Regeneration technology, hydrocarbons are carried to chlorine absorber portion or chlorine tourie with reclaimable catalyst, this to be used as displacement gas using recycle hydrogen
Method bring some problems at the same time, be specially：
First, hydrocarbons are discharged with regeneration vent gas, non-methane hydrocarbon discharge beyond standards in regeneration vent gas are caused；Its
Two, chlorine absorber portion or chlorine tourie are in various degree there are local overheating phenomenon, and when temperature is up to more than 240 DEG C, reclaimable catalyst is deposited
Tendency is being burnt, is burning generation water because low-carbon hydrocarbons exist so that the operation conditions of chlorine absorber portion or chlorine tourie tends to
Deteriorate.In addition, the oil gas on catalyst cannot be blown away such as recycle hydrogen band oil so that the lifting and conveying of catalyst become difficult.
Praxair Technology, Inc (hereinafter referred to as UOP) is one of leading provider of global continuous catalytic reforming device technology.
Its Chinese patent CN1249204C reacts and regenerative system discloses folded stage reactor bottom and is equipped with catalyst granules from reaction
The lower reservations room taken out in device（Reactor catalyst collecting tank）, lower reservations room has cleans from the catalyst in lower reservations room
The hydrogen of hydrocarbon（Reactor displacement gas）Ingress port, lower reservations room allows hydrogen to flow up into bottom reactor.
What Xu Cheng grace was edited for 2006《Catalytic reforming process and engineering》The 392-396 pages discloses reclaimable catalyst the bottom of from
Reactor catalyst collecting tank purges the flow of most oil gas on reclaimable catalyst through displacement gas, and discloses Fig. 7-28
With Fig. 7-29.Before it can be seen that reclaimable catalyst enters catalyst lifting system in figure, totally to be generated urge must be purged through displacement gas
Most oil gas in agent.
Lee into writing for 2001《Catalytic reforming operating guidance》The 104-106 pages knot for disclosing catalyst collection tank
Structure and flow, and point out catalyst collection tank generally using the circulating air purging of preheating and heating.By in Fig. 4-26 of page 106
It can be seen that catalyst collection tank joins together with last reactor, the circulating air purging entrance for displacement is arranged in catalysis
On agent collecting tank, purge gass are flowed out with reaction mass.
The content of the invention
The object of the present invention is to provide a kind of improved method of continuous reformer reactor displacement gas flow, displacement gas by
Recycle hydrogen uses the less source of the gas hydrogen of hydrocarbon-containifirst material instead, bad to solve the recycle hydrogen band more purging effect of hydrocarbon, causes catalyst
Band oil influences lifting and conveying；The operation conditions of reclaimable catalyst chlorine absorber portion or chlorine tourie aggravates and is caused again with hydrocarbon
The raw technical problems such as middle non-methane hydrocarbon discharge beyond standards of dropping a hint.
To achieve the above object, the technical solution adopted by the present invention is：
A kind of improved method of continuous reformer reactor displacement gas flow, it is characterised in that：Hydrocarbon-containifirst material is less
Source of the gas hydrogen be divided into two strands, one as No.1 reactor displacement gas after No.1 reactor displacement gas flow control valve regulation through No.1
Reactor displacement gas heat exchanger exchanges heat to 120~140 DEG C, is purged into second reactor catalyst collection device from second reactor
Oil gas on the catalyst flowed down according to dead weight, the catalyst for blowing away oil gas are promoted to the 3rd reactor breeze way, and displacement gas is with second
The second intermediate heating furnace that reactor reaction product enters together；One puts as No. two reactor displacement gas through No. two reactors
Exchange heat after ventilation flow control valve regulation through No. two reactor displacement gas heat exchangers to 120~140 DEG C, into the 4th reactor catalyst
Collector purging is promoted to catalysis to be generated from oil gas, the catalyst for blowing away oil gas on the catalyst that the 4th reactor is flowed down according to dead weight
Agent separates hopper, the reformation mixed feeding heat exchanger that displacement gas enters with the 4th reactor reaction product.
A kind of improved method of continuous reformer reactor displacement gas flow of the present invention, it is further characterized by：Institute
The less source of the gas hydrogen of hydrocarbon-containifirst material is stated quoted from continuous reformer.
A kind of improved method of continuous reformer reactor displacement gas flow of the present invention, it is further characterized by：Institute
State the less source of the gas hydrogen of hydrocarbon-containifirst material come from reactor reduction section extraction also Primordial Qi drop a hint.
A kind of improved method of continuous reformer reactor displacement gas flow of the present invention, it is further characterized by：Institute
The less source of the gas hydrogen of the hydrocarbon-containifirst material stated, specific component are hydrogeneous >=90% (percent by volume), more than four hydrocarbon content of carbon≤
1.0% (percent by volume), three content≤2.0 of carbon (percent by volume), two content≤3.0 of carbon (percent by volume), remaining is first
Alkane；It is preferred that reduction section drops a hint, reforms pure hydrogen of hydrogen, PSA etc., most preferably reduction section is dropped a hint.
For the reactor being arranged in juxtaposition, each reactor bottom catalyst collection device displacement gas uses hydrocarbon-containifirst instead by recycle hydrogen
The less source of the gas hydrogen of material, preferably to be purged to the catalyst in each reactor bottom catalyst collection device, improves
Presequence reactor catalyst is promoted to next reactor conditions.
The reactor or the reactor of arranged superposed being either arranged in juxtaposition, last reactor bottom catalyst are received
Storage displacement gas uses the less source of the gas hydrogen of hydrocarbon-containifirst material instead by recycle hydrogen, to be received to last reactor bottom catalyst
Reclaimable catalyst in storage is preferably purged, and is improved situation of the reclaimable catalyst with hydrocarbon, is made non-first in regeneration vent gas
Alkanes qualified discharge；Improve the operation conditions of chlorine absorber portion or chlorine tourie at the same time.
By using above-mentioned technical proposal, the invention has the advantages that：
1. purge from last reactor and flowed down according to dead weight as displacement gas using the less source of the gas hydrogen of hydrocarbon-containifirst material
Catalyst on oil gas, the oil gas on reclaimable catalyst can be blown it is more clean, reclaimable catalyst carry band hydrocarbons can be more
It is few, be conducive to improve the operation conditions of chlorine absorber portion or chlorine tourie, reduce the overtemperature hidden danger of chlorine absorber portion or chlorine tourie.
2. purge from upper reactor and urged according to what dead weight flowed down as displacement gas using the less source of the gas hydrogen of hydrocarbon-containifirst material
Oil gas in agent, can blow the oil gas on catalyst more clean, be conducive to catalyst and be promoted to next reactor or regeneration
System.
It is overlapping two-by-two with reference to the accompanying drawings and detailed description with four reactors, two reaction towers typical case arranged side by side
The present invention is described in further detail exemplified by arrangement, but is not intended to limit the use scope of the present invention.
Brief description of the drawings
Fig. 1 is a kind of improved method process flow diagram of continuous reformer reactor displacement gas flow of the present invention；
Fig. 2 shows for a kind of improved method another kind technological process of continuous reformer reactor displacement gas flow of the present invention
It is intended to.
Reference numeral is shown in it：The less source of the gas hydrogen of 1- hydrocarbon-containifirst materials, 2- No.1 reactor displacement gas flow control valves,
3- No.1 reactor displacement gas heat exchangers, 4- second reactor catalyst collection devices, 5- second reactor reaction products, 6- bis-
Reactor displacement gas flow control valve, No. bis- reactor displacement gas heat exchangers of 7-, the 4th reactor catalyst collectors of 8-, 9- the 4th are anti-
Answer device reaction product, 10- also Primordial Qi, 11- reactor reduction sections, 12- also Primordial Qi drops a hint, and 13- also Primordial Qi heat exchangers, 14- is also
Primordial Qi is dropped a hint poor voltage-controlled valve.
Embodiment
The invention will be further described below in conjunction with the accompanying drawings：
As shown in Figure 1, quoted from the less source of the gas hydrogen 1 of the hydrocarbon-containifirst material in device, it is divided into two strands, one is as No.1
Reactor displacement gas exchanges heat to 120 after the adjusting of No.1 reactor displacement gas flow control valve 2 through No.1 reactor displacement gas heat exchanger 3
~140 DEG C, purged into second reactor catalyst collection device 4 from oil gas on the catalyst that second reactor is flowed down according to dead weight,
The catalyst for blowing away oil gas is promoted to the 3rd reactor breeze way, and displacement gas enters with second reactor reaction product 5
Second intermediate heating furnace.One as No. two reactor displacement gas after No. two reactor displacement gas flow control valves 6 are adjusted through No. two
Reactor displacement gas heat exchanger 7 exchanges heat to 120~140 DEG C, is purged into the 4th reactor catalyst collector 8 from the 4th reaction
For device according to oil gas on the catalyst that flows down of dead weight, the catalyst for blowing away oil gas is promoted to reclaimable catalyst separation hopper, displacement gas with
The reformation mixed feeding heat exchanger that 4th reactor reaction product 9 enters together.
As shown in Figure 2, also Primordial Qi 10 enters reactor reduction section 11, after regenerated catalyst is reduced, also Primordial Qi emptying
12 autoreactor reduction section 11 of gas is drawn, and after also Primordial Qi heat exchanger 13 exchanges heat, one is as No.1 reactor displacement gas through one
Number reactor purge gass flow control valve 2 exchanges heat to 120~140 DEG C, into second after adjusting through No.1 reactor displacement gas heat exchanger 3
Reactor catalyst collector 4 purges the catalyst for from oil gas on the catalyst that second reactor is flowed down according to dead weight, blowing away oil gas
It is promoted to the 3rd reactor breeze way, the second intermediate heating furnace that displacement gas enters with second reactor reaction product 5.One
Stock is used as No. two reactor displacement gas after No. two reactor displacement gas flow control valves 6 are adjusted through No. two reactor displacement gas heat exchangers
7 heat exchange purge the catalysis flowed down from the 4th reactor according to dead weight into the 4th reactor catalyst collector 8 to 120~140 DEG C
Oil gas in agent, the catalyst for blowing away oil gas are promoted to reclaimable catalyst separation hopper, and displacement gas is with the 4th reactor reaction product 9
The reformation mixed feeding heat exchanger entered together.Remaining also Primordial Qi is dropped a hint between reacted device reduction section and first reactor
Differential pressure control also Primordial Qi drop a hint poor voltage-controlled valve 14 drain into reform hydrogen air cooler entrance.
Claims (5)
- A kind of 1. improved method of continuous reformer reactor displacement gas flow, it is characterised in that：Hydrocarbon-containifirst material is less Source of the gas hydrogen is divided into two strands, one as No.1 reactor displacement gas after No.1 reactor displacement gas flow control valve regulation it is anti-through No.1 Answer device displacement gas heat exchanger to exchange heat to 120~140 DEG C, into second reactor catalyst collection device purging from second reactor according to Oil gas on the catalyst that dead weight flows down, the catalyst for blowing away oil gas are promoted to the 3rd reactor breeze way, and displacement gas is anti-with second Answer the second intermediate heating furnace that device reaction product enters together；One is replaced as No. two reactor displacement gas through No. two reactors Exchange heat to 120~140 DEG C through No. two reactor displacement gas heat exchangers after air-flow control valve regulation, received into the 4th reactor catalyst Storage purging is promoted to reclaimable catalyst from oil gas, the catalyst for blowing away oil gas on the catalyst that the 4th reactor is flowed down according to dead weight Separate hopper, the reformation mixed feeding heat exchanger that displacement gas enters with the 4th reactor reaction product.
- 2. the improved method of continuous reformer reactor displacement gas flow according to claim 1, it is characterised in that：Institute The less source of the gas hydrogen of hydrocarbon-containifirst material is stated quoted from continuous reformer.
- 3. the improved method of continuous reformer reactor displacement gas flow according to claim 1, it is characterised in that：Institute The less source of the gas hydrogen of the hydrocarbon-containifirst material stated, specific component are hydrogeneous >=90% (percent by volume), more than four hydrocarbon content of carbon≤ 1.0% (percent by volume), three content≤2.0 of carbon (percent by volume), two content≤3.0 of carbon (percent by volume), remaining is Methane.
- 4. the improved method of continuous reformer reactor displacement gas flow according to claim 1, it is characterised in that：Institute State the less source of the gas hydrogen of hydrocarbon-containifirst material come from reactor reduction section extraction also Primordial Qi drop a hint, reform hydrogen or the pure hydrogen of PSA.
- 5. the improved method of continuous reformer reactor displacement gas flow according to claim 1, it is characterised in that：Institute The less source of the gas hydrogen of the hydrocarbon-containifirst material stated is dropped a hint for reduction section.
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| CN201610934828.3A CN108018073A (en) | 2016-11-01 | 2016-11-01 | A kind of improved method of continuous reformer reactor displacement gas flow |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1042559A (en) * | 1988-10-27 | 1990-05-30 | 法国石油公司 | The method of catalytic reforming in several moving bed reactions side by side district |
| US20060213811A1 (en) * | 2005-03-22 | 2006-09-28 | Clay Russell T | Method for operating catalytic reformers |
| CN102295954A (en) * | 2010-06-25 | 2011-12-28 | 中国石油化工股份有限公司 | Counter-current moving bed reforming process device and catalyst conveying method thereof |
| CN105368488A (en) * | 2014-08-21 | 2016-03-02 | 中国石化工程建设有限公司 | Continuous reforming technology of hydrocarbons |
-
2016
- 2016-11-01 CN CN201610934828.3A patent/CN108018073A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1042559A (en) * | 1988-10-27 | 1990-05-30 | 法国石油公司 | The method of catalytic reforming in several moving bed reactions side by side district |
| US20060213811A1 (en) * | 2005-03-22 | 2006-09-28 | Clay Russell T | Method for operating catalytic reformers |
| CN102295954A (en) * | 2010-06-25 | 2011-12-28 | 中国石油化工股份有限公司 | Counter-current moving bed reforming process device and catalyst conveying method thereof |
| CN105368488A (en) * | 2014-08-21 | 2016-03-02 | 中国石化工程建设有限公司 | Continuous reforming technology of hydrocarbons |
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Application publication date: 20180511 |
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