CN103910329A - High-efficiency energy-saving heat exchange novel technology - Google Patents
High-efficiency energy-saving heat exchange novel technology Download PDFInfo
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- CN103910329A CN103910329A CN201310747173.5A CN201310747173A CN103910329A CN 103910329 A CN103910329 A CN 103910329A CN 201310747173 A CN201310747173 A CN 201310747173A CN 103910329 A CN103910329 A CN 103910329A
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- China
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- pipeline
- heat exchange
- interchanger
- tube side
- preheater
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention belongs to the technical field of chemical engineering and relates to a technology of producing hydrogen by methanol cracking. A preheater 101, a heat exchanger 102, a vaporization superheater 103, a converter 104 and a condenser 105 are connected by pipes so that heat of a raw material liquid and heat of converted gas are exchanged multiple times and thus energy consumption is greatly reduced and production efficiency is improved.
Description
Technical field
The present invention is applicable to chemical field, relates to schizolysis hydrogen production plant with methanol.
Background technology
Hydrogen has a purposes widely industrial.In recent years, due to developing rapidly of fine chemistry industry, anthraquinone producing hydrogen peroxide, powder metallurgy, oil hydrogenation, forestry product and agriculture product hydrogenation, biotechnology, refining of petroleum hydrogenation and hydrogen fuel cleaning vehicle etc., pure hydrogen demand is increased rapidly.
To not facilitating the area of hydrogen source, if adopt traditional separating and preparing hydrogen that comes taking petroleum-type, Sweet natural gas or coal as raw material gas making to need huge investment--" being equivalent to synthetic ammonia half ", be only applicable to large-scale consumer.Middle-size and small-size user's brine electrolysis can conveniently make hydrogen, but energy consumption is very large, every cubic metre of reach～6 degree of hydrogen power consumption, and hydrogen purity is undesirable, impurity is many, scale is also restricted simultaneously, and therefore many former producers with water electrolysis hydrogen production undergo technological transformation one after another in recent years, use the operational path that preparing hydrogen by methanol vapour transformation is new instead.
Nowadays, schizolysis hydrogen production plant with methanol is widely used, its basic technology is: first alcohol and water is by necessarily mixing than row, enter convertor with gas phase form, through catalyst effect, methyl alcohol and water will be converted into hydrogen and carbonic acid gas, these devices need cool to pyrolytic conversion gas and enter pressure-swing absorption apparatus after normal temperature and carry out purification processes after twice heat exchange, when twice heat exchange, adopt 2 interchanger classification heat exchange, First interchanger utilizes reforming gas and material benzenemethanol to carry out heat exchange, recovery part heat, vaporize in interchanger for preventing methyl alcohol, the temperature of methyl alcohol outlet is controlled under the vaporization temperature of methyl alcohol under working pressure, at this moment the temperature out of reforming gas is generally in 120 degree left and right, then reforming gas carries out cooling with recirculated cooling water again in condenser, its temperature is reduced in below 40 degree, the heat of gas from converter outlet is not fully utilized like this, and it is larger to consume circulating cooling water consumption, cause plant energy consumption high.
Summary of the invention
The present invention is on the basis of above-mentioned technique, and the defect existing for background technology, provides a kind of energy-efficient heat exchange novel process.
The novel heat exchange technique that this invention is related, mainly comprises: preheater 101, interchanger E102, vaporization superheater 103, convertor 104, condenser 105.Raw material pipeline is connected with preheater 101 tube side entrances, preheater 101 tube side outlets are connected with interchanger 102 shell side entrances by pipeline, interchanger 102 shell side outlets are connected with vaporization superheater 103 shell side entrances by pipeline, the 103 shell side outlets of vaporization superheater are connected by pipeline with convertor 104, convertor 104 tube side outlets are connected with interchanger 102 tube side entrances by pipeline, interchanger 102 tube side outlets are connected with the shell side entrance of preheater 101 by pipeline, the shell side outlet of preheater 101 is connected with the tube side entrance of condenser 105 by pipeline, the tube side outlet of condenser 105 is delivered to cooled reactant gases out-of-bounds by pipeline, thermal oil enters the vaporization tube side of superheater 103 and the shell side of convertor 104 successively by pipeline, then send out-of-bounds by pipeline.
In sum, novel process of the present invention has the following advantages:
Than traditional technology, the present invention has reclaimed the heat of reforming gas more, has reduced thermal oil heat supplied, has reduced the consumption of recirculated cooling water in condenser, has greatly improved device heat utilization rate.And condenser area is less, heat is poor little, longer service life.
Brief description of the drawings
Fig. 1 is the setting drawing of new type heat exchanger provided by the invention.
Claims (5)
1. an energy-efficient heat exchange novel process, comprises preheater 101, interchanger 102, vaporization superheater 103, convertor 104, condenser 105, raw material pipeline is connected with preheater 101 tube side entrances, preheater 101 tube side outlets are connected with interchanger 102 shell side entrances by pipeline, interchanger 102 shell side outlets are connected with vaporization superheater 103 shell side entrances by pipeline, the 103 shell side outlets of vaporization superheater are connected by pipeline with convertor 104, convertor 104 tube side outlets are connected with interchanger 102 tube side entrances by pipeline, interchanger 102 tube side outlets are connected with the shell side entrance of preheater 101 by pipeline, the shell side outlet of preheater 101 is connected with the tube side entrance of condenser 105 by pipeline, the tube side outlet of condenser 105 is delivered to cooled reactant gases out-of-bounds by pipeline, thermal oil enters the vaporization tube side of superheater 103 and the shell side of convertor 104 successively by pipeline, then send out-of-bounds by pipeline.
2. according to energy-efficient heat exchange novel process claimed in claim 1, it is characterized in that: used new type heat exchanger 102, an air chamber has been set up at the top of this interchanger, and methyl alcohol and water mixture after vaporization are assembled at air chamber.
3. according to energy-efficient heat exchange novel process claimed in claim 1, it is characterized in that: the tube side of new type heat exchanger 102 is reforming gas passage, shell side is the mixture channel of methyl alcohol and water.
4. according to energy-efficient heat exchange novel process claimed in claim 1, it is characterized in that: reforming gas enters interchanger 102 and carries out heat exchange with the mixed solution of material benzenemethanol and water, allows mixed solution vaporization in technique.
5. according to energy-efficient heat exchange novel process claimed in claim 1, it is characterized in that: reforming gas enters condenser 105 after going out preheater 101, and this portion temperature can drop to the minimum temperature of processing requirement.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310747173.5A CN103910329A (en) | 2013-12-30 | 2013-12-30 | High-efficiency energy-saving heat exchange novel technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310747173.5A CN103910329A (en) | 2013-12-30 | 2013-12-30 | High-efficiency energy-saving heat exchange novel technology |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103910329A true CN103910329A (en) | 2014-07-09 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310747173.5A Pending CN103910329A (en) | 2013-12-30 | 2013-12-30 | High-efficiency energy-saving heat exchange novel technology |
Country Status (1)
| Country | Link |
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| CN (1) | CN103910329A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104362355A (en) * | 2014-11-07 | 2015-02-18 | 广东合即得能源科技有限公司 | Methanol water hydrogen-making machine and hydrogen-making method thereof |
| CN107758616A (en) * | 2016-08-15 | 2018-03-06 | 成都科特瑞兴科技有限公司 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101700874A (en) * | 2009-09-09 | 2010-05-05 | 张文波 | Hydrogen making method by pressure swing adsorption |
| CN102287917A (en) * | 2011-06-01 | 2011-12-21 | 刘革 | Heating system of methanol hydrogen-production oxidation |
| CN102627259A (en) * | 2012-03-27 | 2012-08-08 | 成都赛普瑞兴科技有限公司 | Method for preparing hydrogen by methanol-water reforming |
| CN202688235U (en) * | 2012-07-11 | 2013-01-23 | 河南开祥精细化工有限公司 | Device for producing formaldehyde by methanol |
-
2013
- 2013-12-30 CN CN201310747173.5A patent/CN103910329A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101700874A (en) * | 2009-09-09 | 2010-05-05 | 张文波 | Hydrogen making method by pressure swing adsorption |
| CN102287917A (en) * | 2011-06-01 | 2011-12-21 | 刘革 | Heating system of methanol hydrogen-production oxidation |
| CN102627259A (en) * | 2012-03-27 | 2012-08-08 | 成都赛普瑞兴科技有限公司 | Method for preparing hydrogen by methanol-water reforming |
| CN202688235U (en) * | 2012-07-11 | 2013-01-23 | 河南开祥精细化工有限公司 | Device for producing formaldehyde by methanol |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104362355A (en) * | 2014-11-07 | 2015-02-18 | 广东合即得能源科技有限公司 | Methanol water hydrogen-making machine and hydrogen-making method thereof |
| CN107758616A (en) * | 2016-08-15 | 2018-03-06 | 成都科特瑞兴科技有限公司 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
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| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 610037 DIO era 1, middle Xing Road, Chengdu, Sichuan, Jinniu District 1401 Applicant after: CHENGDU ZHUOLI RUIXING TECH CO. Address before: 610091, No. 1, No. 88, golden area, No. three Guanghua Road, Guanghua District, Qingyang District, Sichuan, Chengdu, 1739 Applicant before: CHENGDU ZHUOLI RUIXING TECH CO. |
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| COR | Change of bibliographic data | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20140709 |