CN104610058A - Recycling technology for byproduct steam of dimethyl oxalate synthetic process - Google Patents
Recycling technology for byproduct steam of dimethyl oxalate synthetic process Download PDFInfo
- Publication number
- CN104610058A CN104610058A CN201510019635.0A CN201510019635A CN104610058A CN 104610058 A CN104610058 A CN 104610058A CN 201510019635 A CN201510019635 A CN 201510019635A CN 104610058 A CN104610058 A CN 104610058A
- Authority
- CN
- China
- Prior art keywords
- steam
- dimethyl oxalate
- compressor
- pressure
- drum
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a recycling technology for byproduct steam of a dimethyl oxalate synthetic process. According to the recycling technology, dimethyl oxalate steam drums are used for generating steam through heat released through a dimethyl oxalate synthetic reaction, and heat is recovered; a steam condensation line and a steam compression recycling line are adopted, steam compression recycling can guarantee stable heat of a dimethyl oxalate synthetic system, and heat released through the reaction can be effectively used; a multi-section compression and loop control method is adopted, inter-section and tail-end steam discharge can be adopted according to device requirement, required different grades of steam can be obtained selectively, latent heat of low-pressure steam can be recycled effectively, energy loss can be reduced, and good applicability to the dimethyl oxalate synthetic process is realized.
Description
Technical field
The present invention relates to dimethyl oxalate vapor recovery technique field, specifically a kind of recycling technique of dimethyl oxalate synthesis technique byproduct steam.
Background technology
Along with the progressively popularization of dimethyl oxalate method Hydrogenation ethylene glycol Technology, the production technique of ethylene glycol turns to dimethyl oxalate coupling hydro two-step process technology from traditional epoxyethane water is legal.Wherein, dimethyl oxalate carries out gas phase catalytic synthesis by CO and methyl nitrite to obtain, and dimethyl oxalate synthesis reaction temperature is low, and byproduct steam pressure is low; Particularly initial stage byproduct steam only has 106 DEG C, directly delivers to downstream user by pipeline and utilizes very difficult.
The demand of chemical production device to steam is larger, and the steam grade of dimethyl oxalate synthesis by-product is lower, the requirement of direct industrial application can not be met, therefore, how better effectively to utilize this low-pressure steam, also can reduce power loss as far as possible in assurance device steady running, become the emphasis of ethylene glycol and even other close process production techniques concerns.
Adopt traditional interchanger water-cooled heat exchange or the cooling of air cooler air cooling, only can reclaim the water after cooling, the latent heat of this low-pressure steam could not be made full use of, and energy consumption is comparatively large, efficiency is not good as desired yet.
Therefore, still need a kind of novel process system for recycling dimethyl oxalate synthesis by-product low-pressure steam, thus do not lose the latent heat of steam, the continual and steady operation of energy assurance device simultaneously.
summary of the inventionthe object of this invention is to provide a kind of recycling technique of dimethyl oxalate synthesis technique byproduct steam, the problem that prior art interchanger cooling efficiency is low to solve, latent heat does not make full use of.
In order to achieve the above object, the technical solution adopted in the present invention is:
A kind of recycling technique of dimethyl oxalate synthesis technique byproduct steam, it is characterized in that: the low-grade steam of dimethyl oxalate synthesis reactor by-product improves pressure by the mode of vapour compression, retain drum steam evacuation and steam cooling for reflux two kinds of drum steam discharging modes simultaneously, obtained the pressure of required steam by vapour compressor, comprise the following steps:
(1), the waste heat that dimethyl oxalate building-up reactions is released shifts out reactor by reactor drum, reactor cooling pump water by dimethyl oxalate synthesis reactor, enters gas-liquid separation after reactor drum;
(2), the steam of dimethyl oxalate synthesis reactor drum top releasing devaporation pressure recovery utilization under normal circumstances, retain drum steam condenser water cooler, and the emptying of control valve interlocking is set at drum top, to ensure the stable of whole drum vapor pressure;
(3), different series dimethyl oxalate synthesis drum produce steam gather after enter steam buffer tank, governor valve control steam buffer pressure tank is established in steam buffer tank top, and low-pressure steam enters vapour compressor by steam buffer tank;
(4) before, low-pressure steam enters vapour compressor, every section of suction port of compressor arranges steam gas-liquid separator and carries out gas-liquid separation;
(5), vapour compressor adopts multi-stage compression, intersegmentally establishes intersegmental cooler;
(6), the intersegmental and end of vapour compressor sets out gas port, according to steam needs, can be obtained the steam needed by intersegmental or end outlet; Also according to the rotating speed regulating compressor, required steam grade can be obtained;
(7), surge loop of setting up defences between compressor section, the flow of adjustment steam compression system;
(8), steam arranges Vaporized temperature-reducing device after going out vapour compressor, sprays into oiler feed and obtains the suitable temperature of steam.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, is characterized in that: the quantity of steam of described dimethyl oxalate synthesis by-product is 20 ~ 100t/h, and working pressure is 1.0bar(A) ~ 3.0bar(A), 100 ~ 133 DEG C.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, is characterized in that: the reaction heat utilizing dimethyl oxalate to synthesize with Recovery of the hot water, by-product low-pressure steam; By controlling the pressure of drum, ensureing that dimethyl oxalate synthetic catalyst can react in optimum temperature range, avoiding catalyzer temperature runaway.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, it is characterized in that: the steam buffer tank before vapour compressor, collect the steam of multiple serial by-product simultaneously, by the pressure regulator valve of steam buffer tank deck, can ensure that the vapor pressure of multiple dimethyl oxalate synthesizing series by-product stablizes laggard vapour compressor.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, it is characterized in that: the steam gas-liquid separator before vapour compressor is at different levels, greatly can reduce the drop in gas, reduce the possibility of droplet impact vapour compressor impeller, reduce compressor casualty ratio of accidents, the sustainability of plant running can be improved.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, it is characterized in that: vapour compressor adopts multi-stage compression, intersegmentally establish intersegmental cooler, control the temperature of hypomere compressor inlet and the temperature in the surge loop that goes back on defense, avoid vapor temperature too high, also keep certain superheating temperature.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, it is characterized in that: in multistage vapour compressor, vapor pressure can be increased to 0.2 ~ 0.4 MPaG by front two sections of compressions, vapor pressure can be increased to 0.5 ~ 0.7 MpaG or more after adopting multi-stage compression, according to needing situation to carry out selection to arrange hop count to steam, intersegmentally can drawing gas or end goes out vapour, also by changing the rotating speed of compressor, the pressure of vapour compressor battery limit (BL) can be adjusted.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, is characterized in that: by the Surge Prevention System of vapour compressor or the load of adjustment of rotational speed steam compression system changing compressor.
The recycling technique of described a kind of dimethyl oxalate synthesis technique byproduct steam, is characterized in that: by Vaporized temperature-reducing device, sprays into the temperature that oiler feed reduces steam, obtains the suitable temperature entering full factory pipe network grade.
Advantage of the present invention:
The present invention is according to the grade of dimethyl oxalate reactor byproduct steam, adopt vapour compression and vapor condensation two kinds of steam treatment modes, ensure that system stability, and the Lowlevel thermal energy that can effectively utilize system to produce, reclaim heat energy, avoid power loss, to the recycling of dimethyl oxalate synthesis by-product heat, there is good suitability.Adopt the vapor-recovery system in the present invention, the reliability of the whole systems such as dimethyl oxalate synthesis, steam utilization can be improved.
Accompanying drawing explanation
Fig. 1 is the block diagram of present invention process.
Embodiment
Shown in Figure 1, a kind of recycling technique of dimethyl oxalate synthesis technique byproduct steam, the low-grade steam of dimethyl oxalate synthesis reactor by-product improves pressure by the mode of vapour compression, retain drum steam evacuation and steam cooling for reflux two kinds of drum steam discharging modes simultaneously, obtained the pressure of required steam by vapour compressor, comprise the following steps:
(1), the waste heat that dimethyl oxalate building-up reactions is released shifts out reactor by reactor drum, reactor cooling pump water by dimethyl oxalate synthesis reactor, enters gas-liquid separation after reactor drum;
(2), the steam of dimethyl oxalate synthesis reactor drum top releasing devaporation pressure recovery utilization under normal circumstances, retain drum steam condenser water cooler, and the emptying of control valve interlocking is set at drum top, to ensure the stable of whole drum vapor pressure;
(3), different series dimethyl oxalate synthesis drum produce steam gather after enter steam buffer tank, governor valve control steam buffer pressure tank is established in steam buffer tank top, and low-pressure steam enters vapour compressor by steam buffer tank;
(4) before, low-pressure steam enters vapour compressor, every section of suction port of compressor arranges steam gas-liquid separator and carries out gas-liquid separation;
(5), vapour compressor adopts multi-stage compression, intersegmentally establishes intersegmental cooler;
(6), the intersegmental and end of vapour compressor sets out gas port, according to steam needs, can be obtained the steam needed by intersegmental or end outlet; Also according to the rotating speed regulating compressor, required steam grade can be obtained;
(7), surge loop of setting up defences between compressor section, the flow of adjustment steam compression system;
(8), steam arranges Vaporized temperature-reducing device after going out vapour compressor, sprays into oiler feed and obtains the suitable temperature of steam.
The quantity of steam of dimethyl oxalate synthesis by-product is 20 ~ 100t/h, and working pressure is 1.0bar(A) ~ 3.0bar(A), 100 ~ 133 DEG C.
With the reaction heat that Recovery of the hot water utilizes dimethyl oxalate to synthesize, by-product low-pressure steam; By controlling the pressure of drum, ensureing that dimethyl oxalate synthetic catalyst can react in optimum temperature range, avoiding catalyzer temperature runaway.
Steam buffer tank before vapour compressor, collects the steam of multiple serial by-product simultaneously, by the pressure regulator valve of steam buffer tank deck, can ensure that the vapor pressure of multiple dimethyl oxalate synthesizing series by-product stablizes laggard vapour compressor.
Steam gas-liquid separator before vapour compressor is at different levels, greatly can reduce the drop in gas, reduces the possibility of droplet impact vapour compressor impeller, reduces compressor casualty ratio of accidents, can improve the sustainability of plant running.
Vapour compressor adopts multi-stage compression, intersegmentally establishes intersegmental cooler, controls the temperature of hypomere compressor inlet and the temperature in the surge loop that goes back on defense, avoids vapor temperature too high, also keep certain superheating temperature.
In multistage vapour compressor, vapor pressure can be increased to 0.2 ~ 0.4 MPaG by front two sections of compressions, vapor pressure can be increased to 0.5 ~ 0.7 MpaG or more after adopting multi-stage compression, according to needing situation to carry out selection to arrange hop count to steam, can intersegmentally to draw gas or end goes out vapour, also by changing the rotating speed of compressor, the pressure of vapour compressor battery limit (BL) can be adjusted.
By the Surge Prevention System of vapour compressor or the load of adjustment of rotational speed steam compression system changing compressor.
By Vaporized temperature-reducing device, spray into the temperature that oiler feed reduces steam, obtain the suitable temperature entering full factory pipe network grade.
Specific embodiment:
The process gas that upstream workshop section comes enters dimethyl oxalate reactor, under the effect of catalyzer, heat is released in reaction, by dimethyl oxalate reaction cooling pump reaction water coolant, building-up reactions liberated heat is shifted out, the water coolant absorbed after heat enters dimethyl oxalate reactor drum, thus to produce into working pressure be 1.0bar(A) ~ 3bar(A), service temperature is the low-pressure steam of 100 ~ 133 DEG C, byproduct steam amount is for being about 20 ~ 100t/h, and after compression, vapor pressure is 4.0bar(A) ~ 10.0bar(A).
For maintaining the continual and steady operation of dimethyl oxalate building-up reactions, the caloric requirement of reaction is constantly removed, arrange the cooling of drum steam condenser to reclaim and devaporation pressure recovery utilizes two-way pipeline at drum top, and securing point emptying is set at the drum top of each series.Under normal circumstances, the low-pressure steam that each serial dimethyl oxalate synthesis drum produces enters gathering tube, and the steam after gathering enters after steam buffer tank cushions and enters downstream steam recycling system.When needing the work output adjusting downstream steam, the alternative drum condenser condenses that entered by the steam of part drum reclaims; When the dimethyl oxalate synthesis system of certain series break down or system overpressure time, open the blow-off valve of respective series, thus do not affect the steam fed downstream steam compression system of other series; If steam compression system breaks down or repair and maintenance time, close the valve that enters on steam compression system pipeline, open direct blow-off valve, by steam directly in the emptying of height point.Vapor condensation and vapour compression two-way system in parallel are arranged; both selective control downstream steam growing amount can be gone to; reduce the interference between different series dimethyl oxalate synthesis system; the stable of dimethyl oxalate system thermal can be ensured again, guard catalyst can be played, avoid reactor to occur the effect that temperature rises sharply.
When steam compresses in steam compression system, after improving its vapor pressure grade, can steam pipe system be entered, supply full factory other steam user and use.
Enter the low-pressure steam of steam compression system, after first carrying out buffering voltage stabilizing by steam buffer tank, deliver to steam compression system, by steam gas-liquid separator removing drop, the effect of protection compressor can be played.Except the steam after liquid enters vapour compressor, the steam of different pressures grade can be obtained respectively after two sections or three sections of compressions, meet the different needs of Chemical Manufacture to steam.One section intersegmental arranges anti-surge loop and anti-surge valve, for adjusting the load of compressor with two sections, two sections with three.
Between compressor section, outlet is set, according to pipe network need send steam.After multi-stage compression, the steam sent arranges Desuperheating device, enters steam pipe system for user after adjusting temperature as required.
Claims (9)
1. the recycling technique of a dimethyl oxalate synthesis technique byproduct steam, it is characterized in that: the low-grade steam of dimethyl oxalate synthesis reactor by-product improves pressure by the mode of vapour compression, retain drum steam evacuation and steam cooling for reflux two kinds of drum steam discharging modes simultaneously, obtained the pressure of required steam by vapour compressor, comprise the following steps:
(1), the waste heat that dimethyl oxalate building-up reactions is released shifts out reactor by reactor drum, reactor cooling pump water by dimethyl oxalate synthesis reactor, enters gas-liquid separation after reactor drum;
(2), the steam of dimethyl oxalate synthesis reactor drum top releasing devaporation pressure recovery utilization under normal circumstances, retain drum steam condenser water cooler, and the emptying of control valve interlocking is set at drum top, to ensure the stable of whole drum vapor pressure;
(3), different series dimethyl oxalate synthesis drum produce steam gather after enter steam buffer tank, governor valve control steam buffer pressure tank is established in steam buffer tank top, and low-pressure steam enters vapour compressor by steam buffer tank;
(4) before, low-pressure steam enters vapour compressor, every section of suction port of compressor arranges steam gas-liquid separator and carries out gas-liquid separation;
(5), vapour compressor adopts multi-stage compression, intersegmentally establishes intersegmental cooler;
(6), the intersegmental and end of vapour compressor sets out gas port, according to steam needs, can be obtained the steam needed by intersegmental or end outlet; Also according to the rotating speed regulating compressor, required steam grade can be obtained;
(7), surge loop of setting up defences between compressor section, the flow of adjustment steam compression system;
(8), steam arranges Vaporized temperature-reducing device after going out vapour compressor, sprays into oiler feed and obtains the suitable temperature of steam.
2. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, it is characterized in that: the quantity of steam of described dimethyl oxalate synthesis by-product is 20 ~ 100t/h, working pressure is 1.0bar(A) ~ 3.0bar(A), 100 ~ 133 DEG C.
3. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, is characterized in that: the reaction heat utilizing dimethyl oxalate to synthesize with Recovery of the hot water, by-product low-pressure steam; By controlling the pressure of drum, ensureing that dimethyl oxalate synthetic catalyst can react in optimum temperature range, avoiding catalyzer temperature runaway.
4. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, it is characterized in that: the steam buffer tank before vapour compressor, collect the steam of multiple serial by-product simultaneously, by the pressure regulator valve of steam buffer tank deck, can ensure that the vapor pressure of multiple dimethyl oxalate synthesizing series by-product stablizes laggard vapour compressor.
5. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, it is characterized in that: the steam gas-liquid separator before vapour compressor is at different levels, greatly can reduce the drop in gas, reduce the possibility of droplet impact vapour compressor impeller, reduce compressor casualty ratio of accidents, the sustainability of plant running can be improved.
6. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, it is characterized in that: vapour compressor adopts multi-stage compression, intersegmentally establish intersegmental cooler, control the temperature of hypomere compressor inlet and the temperature in the surge loop that goes back on defense, avoid vapor temperature too high, also keep certain superheating temperature.
7. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, it is characterized in that: in multistage vapour compressor, vapor pressure can be increased to 0.2 ~ 0.4 MPaG by front two sections of compressions, vapor pressure can be increased to 0.5 ~ 0.7 MpaG or more after adopting multi-stage compression, according to needing situation to carry out selection to arrange hop count to steam, can intersegmentally to draw gas or end goes out vapour, also by changing the rotating speed of compressor, the pressure of vapour compressor battery limit (BL) can be adjusted.
8. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, is characterized in that: by the Surge Prevention System of vapour compressor or the load of adjustment of rotational speed steam compression system changing compressor.
9. the recycling technique of a kind of dimethyl oxalate synthesis technique byproduct steam according to claim 1, is characterized in that: by Vaporized temperature-reducing device, sprays into the temperature that oiler feed reduces steam, obtains the suitable temperature entering full factory pipe network grade.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510019635.0A CN104610058B (en) | 2015-01-14 | 2015-01-14 | A kind of recycling technique of dimethyl oxalate. synthesis technique byproduct steam |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510019635.0A CN104610058B (en) | 2015-01-14 | 2015-01-14 | A kind of recycling technique of dimethyl oxalate. synthesis technique byproduct steam |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104610058A true CN104610058A (en) | 2015-05-13 |
| CN104610058B CN104610058B (en) | 2016-08-24 |
Family
ID=53144749
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510019635.0A Active CN104610058B (en) | 2015-01-14 | 2015-01-14 | A kind of recycling technique of dimethyl oxalate. synthesis technique byproduct steam |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104610058B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106979513A (en) * | 2016-01-15 | 2017-07-25 | 中国石化工程建设有限公司 | A kind of device and method for comprehensively utilizing reactor drum institute producing steam |
| CN104990336B (en) * | 2015-06-15 | 2020-07-21 | 中国天辰工程有限公司 | High-temperature cooling water system for synthesizing chloroacetic acid |
| CN112197613A (en) * | 2020-09-30 | 2021-01-08 | 四川金象赛瑞化工股份有限公司 | Method and device for recovering steam |
| CN113375133A (en) * | 2021-06-23 | 2021-09-10 | 四川金象赛瑞化工股份有限公司 | High-grade steam production device utilizing melamine production system and method for producing high-grade steam by utilizing high-grade steam production device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0742198A1 (en) * | 1995-05-12 | 1996-11-13 | Ube Industries Limited | Process for continuously producing dimethyl carbonate |
| CN102516031A (en) * | 2011-11-23 | 2012-06-27 | 安徽淮化股份有限公司 | Method and device system for preventing DMO (dimethyl oxalate) from curing in ethylene glycol industrial production |
| CN203238198U (en) * | 2013-03-22 | 2013-10-16 | 中国昆仑工程公司 | System for utilizing waste heat of byproduct low-pressure steam in coal ethylene glycol process |
| CN103467256A (en) * | 2013-08-21 | 2013-12-25 | 江苏凯茂石化科技有限公司 | Formaldehyde production device and method for recycling thermal energy of tail gas by-product steam |
| CN104098441A (en) * | 2014-06-05 | 2014-10-15 | 上海戊正工程技术有限公司 | Technology and device system for producing dimethyl oxalate by high-pressure carbonylation of industrial synthesis gases and producing ethylene glycol through dimethyl oxalate hydrogenation |
-
2015
- 2015-01-14 CN CN201510019635.0A patent/CN104610058B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0742198A1 (en) * | 1995-05-12 | 1996-11-13 | Ube Industries Limited | Process for continuously producing dimethyl carbonate |
| CN102516031A (en) * | 2011-11-23 | 2012-06-27 | 安徽淮化股份有限公司 | Method and device system for preventing DMO (dimethyl oxalate) from curing in ethylene glycol industrial production |
| CN203238198U (en) * | 2013-03-22 | 2013-10-16 | 中国昆仑工程公司 | System for utilizing waste heat of byproduct low-pressure steam in coal ethylene glycol process |
| CN103467256A (en) * | 2013-08-21 | 2013-12-25 | 江苏凯茂石化科技有限公司 | Formaldehyde production device and method for recycling thermal energy of tail gas by-product steam |
| CN104098441A (en) * | 2014-06-05 | 2014-10-15 | 上海戊正工程技术有限公司 | Technology and device system for producing dimethyl oxalate by high-pressure carbonylation of industrial synthesis gases and producing ethylene glycol through dimethyl oxalate hydrogenation |
Non-Patent Citations (1)
| Title |
|---|
| 赵杰丰: "低品质蒸汽的回收和利用", 《小氮肥》, vol. 40, no. 10, 31 October 2012 (2012-10-31), pages 14 - 15 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104990336B (en) * | 2015-06-15 | 2020-07-21 | 中国天辰工程有限公司 | High-temperature cooling water system for synthesizing chloroacetic acid |
| CN106979513A (en) * | 2016-01-15 | 2017-07-25 | 中国石化工程建设有限公司 | A kind of device and method for comprehensively utilizing reactor drum institute producing steam |
| CN112197613A (en) * | 2020-09-30 | 2021-01-08 | 四川金象赛瑞化工股份有限公司 | Method and device for recovering steam |
| CN113375133A (en) * | 2021-06-23 | 2021-09-10 | 四川金象赛瑞化工股份有限公司 | High-grade steam production device utilizing melamine production system and method for producing high-grade steam by utilizing high-grade steam production device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104610058B (en) | 2016-08-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104610058A (en) | Recycling technology for byproduct steam of dimethyl oxalate synthetic process | |
| CN101956061B (en) | Process and device for recovering and recycling protective gas of bell-type bright annealing furnace | |
| CN104086371B (en) | The processing method that in the cyclohexene method preparing cyclohexanone production process, hexalin is separated | |
| CN113526525B (en) | Synthetic ammonia tower and renewable energy source synthetic ammonia system with waste heat step recovery | |
| CN220070763U (en) | Device for separating high-purity hydrogen chloride from byproduct hydrogen chloride of sucralose | |
| CN218853480U (en) | Urea production system for comprehensively utilizing waste heat of steam condensate | |
| CN112239390B (en) | Ethylene cryogenic recovery system | |
| CN213540516U (en) | Water supply heat regeneration system of steam turbine | |
| CN212199062U (en) | Propylene recovery equipment | |
| CN209978018U (en) | Water feeding pump pipeline of three-pressure waste heat boiler | |
| CN203238198U (en) | System for utilizing waste heat of byproduct low-pressure steam in coal ethylene glycol process | |
| CN104177236B (en) | Prepare the apparatus and method of polymethoxy dimethyl ether | |
| CN112409181A (en) | Dimethyl oxalate rectifying device for coal chemical industry | |
| CN203568999U (en) | Reaction separation system and device for preparing polyoxymethylene dimethyl ethers | |
| CN206902051U (en) | A kind of energy conserving system for being applied to methanol-fueled CLC and methanol rectification | |
| CN207047128U (en) | The utilization system of off-gas in industrial propenecarbonyl synthesizer | |
| CN106679243B (en) | Refrigerating system capable of reducing liquid ammonia consumption | |
| CN217549774U (en) | Methanol synthesis system | |
| CN213708185U (en) | Ethylene cryogenic recovery system | |
| CN220002989U (en) | Energy-saving and stably-operated condensation system of carbon five resin first flash tower | |
| CN213207823U (en) | Multistage flash distillation of high temperature high pressure condensate is retrieved well, low pressure superheated steam system | |
| CN216788835U (en) | System for prolonging service life of steam jet pump | |
| CN102876821B (en) | Water supply method for blast-furnace slag water treatment and water supply systems | |
| CN204281641U (en) | Heat pump ethylene recovery system | |
| CN112387217B (en) | System and method for prolonging operating time of methanol synthesis device by heat recovery |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20160406 Address after: Hefei City, Anhui province 230024 Wangjiang Road No. 70 Applicant after: Donghua Engineering Science & Technology Co., Ltd. Applicant after: Beijing Xinggao Chemical Technology Co., Ltd. Address before: Hefei City, Anhui province 230024 Wangjiang Road No. 70 Applicant before: Donghua Engineering Science & Technology Co., Ltd. |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP02 | Change in the address of a patent holder | ||
| CP02 | Change in the address of a patent holder |
Address after: 230088 in the high tech Industrial Development Zone, No. 669, Changjiang West Road, Hefei City, Anhui Province Co-patentee after: BEIJING XINGGAO CHEMICAL TECHNOLOGY Co.,Ltd. Patentee after: EAST CHINA ENGINEERING SCIENCE AND TECHNOLOGY Co.,Ltd. Address before: 230024 No. 70 Wangjiang East Road, Anhui, Hefei Co-patentee before: BEIJING XINGGAO CHEMICAL TECHNOLOGY Co.,Ltd. Patentee before: EAST CHINA ENGINEERING SCIENCE AND TECHNOLOGY Co.,Ltd. |