CN107032300A - A kind of hydrogen production by methanol system of reactor feed temperature stabilization - Google Patents
A kind of hydrogen production by methanol system of reactor feed temperature stabilization Download PDFInfo
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- CN107032300A CN107032300A CN201710312587.3A CN201710312587A CN107032300A CN 107032300 A CN107032300 A CN 107032300A CN 201710312587 A CN201710312587 A CN 201710312587A CN 107032300 A CN107032300 A CN 107032300A
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- heat exchanger
- oil
- heat
- reactor
- reaction module
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
- C01B3/326—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents characterised by the catalyst
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1217—Alcohols
- C01B2203/1223—Methanol
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/141—At least two reforming, decomposition or partial oxidation steps in parallel
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/148—Details of the flowsheet involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The present invention relates to a kind of hydrogen production by methanol system of reactor feed temperature stabilization, it includes the oil pump being sequentially communicated by heat conducting oil pipe, first heat transfer oil heater, First Heat Exchanger, first reaction module, second heat transfer oil heater, second reaction module and the second heat exchanger, between First Heat Exchanger and the second heat exchanger, connected between First Heat Exchanger and the first reaction module and between First Heat Exchanger and the second reaction module by feedstock transportation pipeline, reaction raw materials are successively through flowing through after the heat-conducting oil heating of the second heat exchanger and First Heat Exchanger heats up while sending into the first reaction module and the second reaction module.Beneficial effects of the present invention are that raw material is through two heat exchanger gradient-heateds, and into temperature stabilization during reactor, the quality of reaction product is preferable；Conduction oil can reduce heater power, so as to avoid heat conduction oil temperature too high and coking by two heaters, two sections of heating.
Description
Technical field
The invention belongs to chemical field, and in particular to a kind of hydrogen production by methanol system of reactor feed temperature stabilization.
Background technology
To reduce the energy consumption in Chemical Manufacture and reducing cost, it is referred to as with replacement " water electrolysis hydrogen production " of electricity-eating tiger
Technique, hydrogen from methyl alcohol turns into a kind of important method for obtaining high-purity hydrogen.Methanol is with vapor in certain temperature, pressure condition
Down by catalyst, in the presence of catalyst, occur methanol decomposition reaction and the transformationreation of carbon monoxide, generate hydrogen and two
Carbonoxide, this gas solid catalytic reaction system for being component more than one, reacting more.Methanol steam reforming is the endothermic reaction, existing
Hydrogen production units by carbinol reaction temperature is typically by material gasification stove and reactor thermal conductivity deep fat Heating Furnace Control (as shown in figure 1, Fig. 1
Middle right side label 11 is material gasification stove), i.e., raw material is passed through in reactor after material gasification furnace gas, and reactor is by through heat conduction
The heated conduction oil supply response institute calorific requirement of oily heating furnace, in actual mechanical process, feeding temperature at reactor inlet
The problem of in the presence of fluctuating larger, and then cause reactor batch temperature to be difficult to control, reaction product does not reach expected requirement.
The content of the invention
The technical problems to be solved by the invention are to provide a kind of hydrogen production by methanol system of reactor feed temperature stabilization, its
Transforming material gasification stove as heat transfer oil heater and two are set up on conduction oil pipeline is used for what raw material exchanged heat with conduction oil
Heat exchanger, so as to ensure that temperature is stablized relatively when raw material enters reactor, so that reaction product reaches expected requirement.
The technical scheme that the present invention solves above-mentioned technical problem is as follows：A kind of hydrogen from methyl alcohol of reactor feed temperature stabilization
System, its oil pump for including being sequentially communicated by heat conducting oil pipe, the first heat transfer oil heater, First Heat Exchanger, the first reaction
Module, the second heat transfer oil heater, the second reaction module and the second heat exchanger, the outlet of the oil pump by heat conducting oil pipe with
The first heat transfer oil heater connection, the entrance of the oil pump is connected by heat conducting oil pipe with second heat exchanger, institute
State between First Heat Exchanger and second heat exchanger, it is between the First Heat Exchanger and first reaction module and described
Connected between First Heat Exchanger and second reaction module by feedstock transportation pipeline, reaction raw materials are described through flowing through successively
First reaction module and institute are sent into after the heat-conducting oil heating heating of second heat exchanger and the First Heat Exchanger simultaneously
State the second reaction module.
On the basis of above-mentioned technical proposal, the present invention can also do following improvement.
Further, first reaction module and second reaction module are made up of several reactors respectively, each
The bottom of the reactor is equipped with heat conductive oil inlet and reacting product outlet, and the top of each reactor is equipped with heat conduction
Oil export and reaction raw materials entrance, conduction oil are corresponding through first reaction module respectively after First Heat Exchanger outflow
The heat conductive oil inlet of several reactor lower parts flows into the reactor, is then flowed out through corresponding conduction oil outlet described
Reactor simultaneously flows into second heat transfer oil heater after converging, conduction oil after second heat transfer oil heater outflow respectively
Heat conductive oil inlet through several corresponding reactor lower parts of second reaction module flows into the reactor, Ran Houjing
Corresponding conduction oil outlet flows out and second heat exchanger is flowed into after converging, reaction raw materials successively through second heat exchanger and
The original of first reaction module and several corresponding reactors of the second reaction module is flowed into after First Heat Exchanger heating simultaneously
Expect entrance.
Further, first reaction module and the second reaction module are made up of one or two reactor respectively, described
The reactor quantity that first reaction module and the second reaction module are included is equal.It is preferred that, the first reaction module and the second reaction
Module each includes two reactors.
Further, cut-off it has been independently arranged on the feedstock transportation pipeline of the reaction raw materials porch of each reactor
Valve.
Further, independently set on the heat conducting oil pipe at the heat conductive oil inlet and conduction oil outlet of each reactor
It is equipped with stop valve.
Further, the First Heat Exchanger, the second heat exchanger and reactor include tube side and shell side, wherein reaction raw materials
Walk shell side and conduction oil walks tube side.
Further, triple valve, the threeway are provided with the heat-conducting oil pipes between the oil pump and second heat exchanger
Three openings of valve connect the oil pump, second heat exchanger and heat conduction oil tank by heat-conducting oil pipes respectively.
Further, it is connected with gs-oil separator on the heat-conducting oil pipes between the triple valve and second heat exchanger.If
The purpose for putting gs-oil separator is that volatile part is changed into gas during circulating-heating when the quality of conduction oil is bad
Body, is discharged during by gs-oil separator, to eliminate it to hydronic adverse effect.
Compared with prior art, the beneficial effects of the invention are as follows：
1) it transform original material gasification stove as heat transfer oil heater and retains original heat transfer oil heater (first leads
Deep fat heating furnace and the second heat transfer oil heater), while setting up two is used for the heat exchanger that is exchanged heat with raw material of conduction oil (first changes
Hot device and the second heat exchanger), it is ensured that multiple reactors are reacted (some reactors of the first reaction module and second simultaneously
Some reactors of reaction module), raw material enters before reactor, first passes around the conduction oil (temperature flowed out by the second reaction module
Degree it is relatively low) preheated in the second heat exchanger, then again by the first heat transfer oil heater outflow conduction oil (temperature compared with
It is high) suitable temperature is heated in First Heat Exchanger, finally it is passed through in reactor and reacts, reaction raw materials reaches pre- through heating up twice
Fixed temperature range, it is ensured that reactor feed temperature is relatively stable, overcomes reactor feed temperature fluctuation in the prior art
Problem.
2) all reactors are divided into two groups, by the first heat transfer oil heater and the second heat transfer oil heater to conduction oil
Two sections of heating are taken, the first heat transfer oil heater carries out first paragraph heating to conduction oil, then conduction oil flows into the first reaction mould
Multiple reactors in block supply its interior endothermic heat of reaction, and the heat conduction oil temperature reduction of the first reaction module outflow is now led by second
Deep fat heating furnace carries out second segment heating to conduction oil, and then conduction oil flows into multiple reactors of the second reaction module and supplies it
Interior endothermic heat of reaction, two sections of heating can ensure that multiple reactors are simultaneously efficient and carry out hydrogen from methyl alcohol reaction, while reducing conduction oil
The power (power of the heat transfer oil heater heated in particular for second segment) of heating furnace, can be prevented effectively from conduction oil because of temperature
The too high and risk of coking.
Brief description of the drawings
Fig. 1 originally directly heats the hydrogen production by methanol system that reactor is passed through after raw material using feed vaporization device in the prior art
Process chart；
A kind of process chart of the hydrogen production by methanol system for reactor feed temperature stabilization that Fig. 2 inventions are provided.
In accompanying drawing, the list of parts representated by each label is as follows：
1. oil pump；2. the first heat transfer oil heater；3. First Heat Exchanger；4. the first reaction module；5. the second conduction oil adds
Hot stove；6. the second reaction module；7. the second heat exchanger；8. reactor；9. triple valve；10. heat conduction oil tank；11. feed vaporization
Stove.
Embodiment
The principle and feature of the present invention are described below in conjunction with drawings and the specific embodiments, example is served only for solution
The present invention is released, the scope of the present invention is not intended to limit.
As shown in Fig. 2 the present invention provides a kind of hydrogen production by methanol system of reactor feed temperature stabilization, it is included by leading
Oil pump 1 that hot oil pipeline is sequentially communicated, the first heat transfer oil heater 2, First Heat Exchanger 3, the first reaction module 4, the second heat conduction
Oily heating furnace 5, the second reaction module 6 and the second heat exchanger 7, the outlet of the oil pump 1 passes through heat conducting oil pipe and described first
Heat transfer oil heater 2 is connected, and the entrance of the oil pump 1 is connected by heat conducting oil pipe with second heat exchanger 7, and described first
Between heat exchanger 3 and second heat exchanger 7, between the First Heat Exchanger 3 and first reaction module 4 and described
Connected between one heat exchanger 3 and second reaction module 6 by feedstock transportation pipeline, reaction raw materials are described through flowing through successively
The He of the first reaction module 4 is sent into after the heat-conducting oil heating heating of second heat exchanger 7 and the First Heat Exchanger 3 simultaneously
Second reaction module 6.First reaction module and the second reaction module outline part in figure for dotted line.
Further, first reaction module 4 and second reaction module 6 are made up of several reactors 8 respectively, often
The bottom of the individual reactor 8 is equipped with heat conductive oil inlet and reacting product outlet, and the top of each reactor 8 is equipped with
Conduction oil outlet and reaction raw materials entrance, conduction oil by the First Heat Exchanger 3 flow out after respectively through first reaction module 4
The heat conductive oil inlet of several corresponding bottoms of reactor 8 flows into the reactor 8, then through corresponding conduction oil outlet
Flow out the reactor 8 and second heat transfer oil heater 5 is flowed into after converging, conduction oil is by second heat transfer oil heater
Described in the heat conductive oil inlet through several corresponding bottoms of reactor 8 of second reaction module 6 is flowed into respectively after 5 outflows
Reactor 8, then flows out through corresponding conduction oil outlet and flows into second heat exchanger 7 after converging, reaction raw materials are passed through successively
6 pairs of 4 and second reaction module of the first reaction module is flowed into after second heat exchanger 7 and First Heat Exchanger 3 heating simultaneously
The feed(raw material)inlet for several reactors 8 answered.
Further, the reaction module 6 of the first reaction module 4 and second is made up of one or two reactor 8 respectively, institute
State the quantity of reactor 8 that the first reaction module 4 and the second reaction module 6 include equal.
Further, it has been independently arranged and has cut on the feedstock transportation pipeline of the reaction raw materials porch of each reactor 8
Only valve.
Further, it is independent on the heat conducting oil pipe at the heat conductive oil inlet and conduction oil outlet of each reactor 8
It is provided with stop valve.
Further, the First Heat Exchanger 3, the second heat exchanger 7 and reactor 8 include tube side and shell side, wherein reacting
Raw material walks shell side and conduction oil walks tube side.
Further, triple valve 9, described three are provided with the heat-conducting oil pipes between the oil pump 1 and second heat exchanger 7
Three openings of port valve 9 connect the oil pump 1, second heat exchanger 7 and heat conduction oil tank 10 by heat-conducting oil pipes respectively.If
Put heat conduction oil tank, easy access and replacing conduction oil.
Factory's actual production shows that improved hydrogen production by methanol system (shown in Fig. 2) is than the hydrogen production by methanol system before transformation
(shown in Fig. 1), production efficiency is higher, and the quality of product is more stable, is obviously reduced, changes before the fluctuation ratio transformation of bed temperature in reactor
The power for making rear heat transfer oil heater is effectively reduced, and conduction oil is because being heated to high temperature and the situation of coking is significantly reduced.
The foregoing is only presently preferred embodiments of the present invention, be not intended to limit the invention, it is all the present invention spirit and
Within principle, any modification, equivalent substitution and improvements made etc. should be included in the scope of the protection.
Claims (8)
1. a kind of hydrogen production by methanol system of reactor feed temperature stabilization, it is characterised in that including by heat conducting oil pipe successively
Oil pump (1), the first heat transfer oil heater (2), First Heat Exchanger (3), the first reaction module (4), the second conduction oil of connection add
Hot stove (5), the second reaction module (6) and the second heat exchanger (7), the outlet of the oil pump (1) by heat conducting oil pipe with it is described
First heat transfer oil heater (2) is connected, and the entrance of the oil pump (1) is connected by heat conducting oil pipe and second heat exchanger (7)
It is logical, between the First Heat Exchanger (3) and second heat exchanger (7), the First Heat Exchanger (3) react mould with described first
Connected between block (4) and between the First Heat Exchanger (3) and second reaction module (6) by feedstock transportation pipeline
Logical, reaction raw materials are same after the heat-conducting oil heating of second heat exchanger (7) and the First Heat Exchanger (3) heats up through flowing through successively
When send into first reaction module (4) and second reaction module (6).
2. the hydrogen production by methanol system of a kind of reactor feed temperature stabilization according to claim 1, it is characterised in that described
First reaction module (4) and second reaction module (6) are made up of several reactors (8) respectively, each reactor
(8) bottom is equipped with heat conductive oil inlet and reacting product outlet, and the top of each reactor (8) is equipped with conduction oil and gone out
Mouth and reaction raw materials entrance, conduction oil is after the First Heat Exchanger (3) outflow respectively through first reaction module (4) correspondence
The heat conductive oil inlets of several reactor (8) bottoms flow into the reactor (8), then through corresponding conduction oil outlet
Flow out the reactor (8) and second heat transfer oil heater (5) is flowed into after converging, conduction oil is added by second conduction oil
Conduction oil after hot stove (5) outflow respectively through several corresponding reactor (8) bottoms of second reaction module (6) enters
Mouthful the reactor (8) is flowed into, is then flowed out through corresponding conduction oil outlet and flow into second heat exchanger (7) after converging,
Reaction raw materials flow into first reaction module simultaneously after second heat exchanger (7) and First Heat Exchanger (3) heating successively
(4) and several corresponding reactors (8) of the second reaction module (6) feed(raw material)inlet.
3. the hydrogen production by methanol system of a kind of reactor feed temperature stabilization according to claim 2, it is characterised in that described
First reaction module (4) and the second reaction module (6) are made up of one or two reactor (8) respectively, the first reaction mould
Reactor (8) quantity that block (4) and the second reaction module (6) are included is equal.
4. the hydrogen production by methanol system of a kind of reactor feed temperature stabilization according to claim 2, it is characterised in that each
The reaction raw materials porch of the reactor (8) has been independently arranged stop valve.
5. the hydrogen production by methanol system of a kind of reactor feed temperature stabilization according to claim 2, it is characterised in that each
Stop valve has been independently arranged at the heat conductive oil inlet and conduction oil outlet of the reactor (8).
6. a kind of hydrogen production by methanol system of reactor feed temperature stabilization according to any one of claim 2 to 5, its feature
It is, the First Heat Exchanger (3), the second heat exchanger (7) and reactor (8) include tube side and shell side, wherein reaction raw materials
Walk shell side and conduction oil walks tube side.
7. a kind of hydrogen production by methanol system of reactor feed temperature stabilization according to any one of claim 1 to 5, its feature
It is, triple valve (9), the triple valve is provided with the heat-conducting oil pipes between the oil pump (1) and second heat exchanger (7)
(9) three openings connect the oil pump (1), second heat exchanger (7) and heat conduction oil tank by heat-conducting oil pipes respectively
(10)。
8. the hydrogen production by methanol system of a kind of reactor feed temperature stabilization according to claim 7, it is characterised in that described
Gs-oil separator is connected with heat-conducting oil pipes between triple valve (9) and second heat exchanger (7).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710312587.3A CN107032300B (en) | 2017-05-05 | 2017-05-05 | A kind of hydrogen production by methanol system that reactor feed temperature is stable |
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| CN201710312587.3A CN107032300B (en) | 2017-05-05 | 2017-05-05 | A kind of hydrogen production by methanol system that reactor feed temperature is stable |
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| CN107032300B CN107032300B (en) | 2019-04-26 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109597446A (en) * | 2019-01-07 | 2019-04-09 | 中氢新能技术有限公司 | A kind of high temperature methanol hydrogen manufacturing temperature control constant temperature method |
| CN110627017A (en) * | 2019-10-30 | 2019-12-31 | 苏州海连净化设备有限公司 | Methanol pyrolysis hydrogen production device |
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| CN205634877U (en) * | 2016-05-09 | 2016-10-12 | 中国船舶重工集团公司第七一二研究所 | A heating device for methyl alcohol reformation hydrogen generation |
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2017
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| CN101559342A (en) * | 2009-05-12 | 2009-10-21 | 石家庄正元塔器设备有限公司 | Gas-solid catalytic reaction heat exchange device and reaction heat exchange process |
| CN101708821A (en) * | 2009-12-08 | 2010-05-19 | 四川亚联高科技股份有限公司 | Methanol steam hydrogen production technology by using catalytic combustion flue gas as heat source |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109597446A (en) * | 2019-01-07 | 2019-04-09 | 中氢新能技术有限公司 | A kind of high temperature methanol hydrogen manufacturing temperature control constant temperature method |
| CN110627017A (en) * | 2019-10-30 | 2019-12-31 | 苏州海连净化设备有限公司 | Methanol pyrolysis hydrogen production device |
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| CN107032300B (en) | 2019-04-26 |
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