CN103044265B - Device and method for producing high-concentration trimethylamine hydrochloride - Google Patents
Device and method for producing high-concentration trimethylamine hydrochloride Download PDFInfo
- Publication number
- CN103044265B CN103044265B CN201210563480.3A CN201210563480A CN103044265B CN 103044265 B CN103044265 B CN 103044265B CN 201210563480 A CN201210563480 A CN 201210563480A CN 103044265 B CN103044265 B CN 103044265B
- Authority
- CN
- China
- Prior art keywords
- hydrochloric acid
- hydrogen chloride
- trimethylamine hydrochloride
- trimethylamine
- reactor
- 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.)
- Expired - Fee Related
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a device for producing high-concentration trimethylamine hydrochloride, which comprises a hydrochloric acid concentration absorber, a hydrochloric acid concentration adsorption tank, a primary reactor, a hydrogen chloride absorber, a hydrogen chloride adsorption tank, a secondary reactor and a salt forming vessel. The invention also discloses a method for producing the high-concentration trimethylamine hydrochloride, which comprises the following steps of: firstly, circulating and concentrating hydrochloric acid and hydrogen chloride in the hydrochloric acid concentration absorber and the hydrochloric acid concentration adsorption tank, then entering into the primary reactor, reacting with trimethylamine, entering the hydrogen chloride absorber after reaction, circulating the trimethylamine hydrochloride and the hydrogen chloride between the hydrogen chloride absorber and the hydrogen chloride adsorption tank, then entering the secondary reactor, reacting with the trimethylamine, conveying into the salt forming vessel after reaction and outputting. By utilizing the device and the method, the high-concentration trimethylamine hydrochloride (which can reach 67-70 percent) can be produced, the steps are simple, the cost is low, and the production of a downstream choline chloride product is facilitated, therefore, the device and the method can be popularized and applied.
Description
Technical field
The present invention relates to a kind of device and method of producing high density trimethylamine hydrochloride, belong to Chemicals production field.
Background technology
At present, trimethylamine hydrochloride is produced and generally to be adopted 31% technical hydrochloric acid to react with 99.7～99.8% Trimethylamine 99, and the trimethylamine hydrochloride solution that output concentration is 53%～54%, is directly used in feed additive industry production choline chloride 60.But 53%～54% trimethylamine hydrochloride is directly used in the production of choline chloride 60, the choline chloride solution degree of output is 62%～63%, and concentration is low, and manufacturing enterprise need to carry out further evaporation concentration to improve the concentration of the finished product, complex steps, and cost is higher.If can directly adopt the trimethylamine hydrochloride of higher concentration to produce choline chloride 60, can reduce the concentrated process of choline chloride 60, even by evaporation concentration, just can directly not obtain the choline chloride 60 product of expectation concentration.In prior art and have no the report relevant for the trimethylamine hydrochloride of production high density.
Summary of the invention
For above-mentioned prior art, the invention provides a kind of device of producing high density trimethylamine hydrochloride, and the method for production high density trimethylamine hydrochloride.
The present invention is achieved by the following technical solutions:
A kind of device of producing high density trimethylamine hydrochloride, comprise hydrochloric acid concentrate resorber, hydrochloric acid concentrate absorption cell, A reactor, hydrogen chloride absorption device, hydrogen chloride absorption groove, second reactor and become salt oven, wherein, hydrochloric acid concentrate absorber bottom is connected with hydrochloric acid concentrate absorption cell top; Hydrochloric acid concentrate absorption cell bottom is connected with A reactor bottom with hydrochloric acid concentrate absorber overhead respectively, and connecting pipeline is provided with recycle pump and control valve; A reactor top is connected with hydrogen chloride absorption device top; Hydrogen chloride absorption device bottom is connected with hydrogen chloride absorption groove top; Hydrogen chloride absorption trench bottom is connected with second reactor bottom with hydrogen chloride absorption device top respectively, and connecting pipeline is provided with recycle pump and control valve; Second reactor top is connected with becoming salt oven top; Become between salt oven top and bottom and be provided with circulation line, circulation line is provided with recycle pump and trimethylamine hydrochloride finished product pipeline; Hydrochloric acid concentrate absorber overhead and hydrogen chloride absorption device top are all connected with hydrogen chloride gas pipeline; Hydrochloric acid concentrate absorber overhead is connected with hydrochloric acid pipeline; On hydrochloric acid concentrate absorption cell and hydrogen chloride absorption groove, be all connected with tail gas recycle pipeline; A reactor and second reactor bottom are all connected with Trimethylamine 99 pipeline; Described connection is pipeline and connects.
Described one-tenth salt oven top is connected with hydrochloric acid pipeline and Trimethylamine 99 pipeline.
Described hydrochloric acid concentrate resorber is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 620 * 5240, and heat interchanging area is 60m
2, access arrangement concentration of hydrochloric acid is 31%, and transport pipe nominal diameter is DN50, and hydrogenchloride purity is 95～96%, and transport pipe nominal diameter is DN200, after concentrate, concentration of hydrochloric acid increases to 34～35%.
Described A reactor is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 886 * 6564, and heat interchanging area is 120m
2, access arrangement concentration of hydrochloric acid is 34～35%, Trimethylamine 99 purity is 99.7～99.8%, and transport pipe nominal diameter is DN50, and control pressure is at < 0.2MPa, and after concentrate, trimethylamine hydrochloride concentration increases to 57～58.6%.
Described hydrogen chloride absorption device is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 620 * 5240, and heat interchanging area is 60m
2, access arrangement Trimethylamine 99 concentration of hydrochloric acid is 57～58.6%, and transport pipe nominal diameter is DN65, and hydrogenchloride purity is 95～96%, and transport pipe nominal diameter is DN200, after absorbing, trimethylamine hydrochloride pH value reaches 1～2.
Described second reactor is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 886 * 6564, and heat interchanging area is 120m
2, access arrangement trimethylamine hydrochloride pH value 1～2, Trimethylamine 99 purity is 99.7～99.8%, and transport pipe nominal diameter is DN50, and control pressure is at < 0.2MPa, and after concentrate, trimethylamine hydrochloride concentration increases to 67～70%.
Described hydrochloric acid concentrate absorption cell, hydrogen chloride absorption groove material are glass reinforced plastic, and specification is ￠ 1350 * 2100, and volume is 3.7m
2.
Described one-tenth salt oven is jacketed lass lining enclosed reactor, housing parameter: use temperature: 100 ℃; Chuck parameter: media name: recirculated cooling water, use temperature :≤60, volume 8m
3.
Described recycle pump is magnetic drive pump, flow: 30m
3∕ h, lift: 20m.
A kind of method of producing high density trimethylamine hydrochloride, step is as follows: first, 31% hydrochloric acid and 95～96% hydrogenchloride are at hydrochloric acid concentrate resorber, juice circulation between hydrochloric acid concentrate absorption cell, when concentration of hydrochloric acid increases to 34～35%, enter A reactor, the Trimethylamine 99 that is 99.7～99.8% with purity reacts, reacted trimethylamine hydrochloride (trimethylamine hydrochloride concentration is 57～58.6%) enters hydrogen chloride absorption device, trimethylamine hydrochloride and hydrogenchloride are at hydrogen chloride absorption device, between hydrogen chloride absorption groove, circulate, the abundant absorbing hydrogen chloride of trimethylamine hydrochloride, reduce pH value, until trimethylamine hydrochloride pH value, be down to 1～2 o'clock, enter second reactor, the Trimethylamine 99 that is 99.7～99.8% with concentration reacts, after reaction, trimethylamine hydrochloride concentration can reach 67～70%, send into into salt oven, then trimethylamine hydrochloride is exported by trimethylamine hydrochloride finished product pipeline, the tail gas producing is sent into tail gas absorption tank by tail gas recycle pipeline and is reclaimed.
Described trimethylamine hydrochloride enters into after salt oven, for guaranteeing qualified product, can in one-tenth salt oven, add micro-Trimethylamine 99 or/and salt acid for adjusting pH value is adjusted to required pH(as pH6.5～7).
Percentage ratio described above is mass percent.
Utilize apparatus and method of the present invention can produce the trimethylamine hydrochloride of high density, step is simple, with low cost, and the concentration of trimethylamine hydrochloride product can reach 67～70%.Production method of the present invention, improved the concentration of trimethylamine hydrochloride, facilitate the production of downstream choline chloride 60 product (to save evaporation link, steam saving, producing choline chloride 60 per ton can steam saving 200Kg, shortens simultaneously and produces choline chloride 60 technical process), can also reduce the costs of transportation and management of unit product, cost is low, can apply.
Accompanying drawing explanation
Fig. 1 is the structural representation of the device of production high density trimethylamine hydrochloride of the present invention.
Fig. 2 is the process flow sheet (in figure, arrow is depicted as the flow direction of material in pipeline) of the method for production high density trimethylamine hydrochloride of the present invention.
Wherein, 1, hydrochloric acid concentrate resorber; 2, hydrochloric acid concentrate absorption cell; 3, A reactor; 4, hydrogen chloride absorption device; 5, hydrogen chloride absorption groove; 6, second reactor; 7, become salt oven; 8, recycle pump;
A, hydrogen chloride gas pipeline; B, hydrochloric acid pipeline; C, circulation water inlet; D circulating backwater; E, 34～35% hydrochloric acid; F, Trimethylamine 99 pipeline; G, 57～58.6% trimethylamine hydrochlorides; The trimethylamine hydrochloride of H, pH1～2; I, 67～70% trimethylamine hydrochloride; J, trimethylamine hydrochloride finished product pipeline; K, tail gas recycle pipeline.
Embodiment
Below in conjunction with drawings and Examples, the present invention is further illustrated.
Embodiment 1
A kind of device of producing high density trimethylamine hydrochloride, comprise hydrochloric acid concentrate resorber 1, hydrochloric acid concentrate absorption cell 2, A reactor 3, hydrogen chloride absorption device 4, hydrogen chloride absorption groove 5, second reactor 6 and become salt oven 7, as shown in Figure 1, wherein, hydrochloric acid concentrate resorber 1 bottom is connected with hydrochloric acid concentrate absorption cell 2 tops; Hydrochloric acid concentrate absorption cell 2 bottoms are connected with A reactor 3 bottoms with hydrochloric acid concentrate resorber 1 top respectively, and connecting pipeline is provided with recycle pump 8 and control valve; A reactor 3 tops are connected with hydrogen chloride absorption device 4 tops; Hydrogen chloride absorption device 4 bottoms are connected with hydrogen chloride absorption groove 5 tops; Hydrogen chloride absorption groove 5 bottoms are connected with second reactor 6 bottoms with hydrogen chloride absorption device 4 tops respectively, and connecting pipeline is provided with recycle pump 8 and control valve; Second reactor 6 tops are connected with becoming salt oven 7 tops; Become between salt oven 7 tops and bottom and be provided with circulation line, circulation line is provided with recycle pump 8 and trimethylamine hydrochloride finished product pipeline J; Hydrochloric acid concentrate resorber 1 top and hydrogen chloride absorption device 4 tops are all connected with hydrogen chloride gas pipeline A; Hydrochloric acid concentrate resorber 1 top is connected with hydrochloric acid pipeline B; On hydrochloric acid concentrate absorption cell 2 and hydrogen chloride absorption groove 5, be all connected with tail gas recycle pipeline K; A reactor 3 and second reactor 6 bottoms are all connected with Trimethylamine 99 pipeline F; Become salt oven 7 tops to be connected with hydrochloric acid pipeline B and Trimethylamine 99 pipeline F; Described connection is pipeline and connects.
Utilize the method for said apparatus production high density trimethylamine hydrochloride, schema as shown in Figure 2, step is as follows: first, 31% hydrochloric acid (B carries by hydrochloric acid pipeline) and 95～96% hydrogenchloride (A carries by hydrogen chloride gas pipeline) are at hydrochloric acid concentrate resorber 1, juice circulation between hydrochloric acid concentrate absorption cell 2, until concentration of hydrochloric acid, increase in 34～35%(Fig. 2 shown in E) time, enter A reactor 3, the Trimethylamine 99 that is 99.7～99.8% with purity (F carries by Trimethylamine 99 pipeline) reacts, (trimethylamine hydrochloride concentration is 57～58.6% for reacted trimethylamine hydrochloride, in Fig. 2 shown in G) enter hydrogen chloride absorption device 4, trimethylamine hydrochloride and hydrogenchloride (by hydrogen chloride gas pipeline, A carries) are at hydrogen chloride absorption device 4, circulation between hydrogen chloride absorption groove 5, the abundant absorbing hydrogen chloride of trimethylamine hydrochloride, reduce pH value, until trimethylamine hydrochloride pH value, be down in 1～2(Fig. 2 shown in H) time, enter second reactor 6, the Trimethylamine 99 that is 99.7～99.8% with concentration (F carries by Trimethylamine 99 pipeline) reacts, after reaction, trimethylamine hydrochloride concentration can reach in 67～70%(Fig. 2 shown in I), send into into salt oven 7, for guaranteeing qualified product, to becoming in salt oven to add micro-Trimethylamine 99 (F carries by Trimethylamine 99 pipeline) or/and hydrochloric acid (B carries by hydrochloric acid pipeline) regulates pH value, be adjusted to required pH6.5～7, then trimethylamine hydrochloride is exported by trimethylamine hydrochloride finished product pipeline J, the tail gas producing is sent into tail gas absorption tank by tail gas recycle pipeline K and is reclaimed.
Described hydrochloric acid concentrate resorber is graphite heat exchanger, and heat-eliminating medium is recirculated water (recirculated water refluxes by intake C and circulating backwater D of circulation), and specification is ￠ 620 * 5240, and heat interchanging area is 60m
2, access arrangement concentration of hydrochloric acid is 31%, and transport pipe nominal diameter is DN50, and hydrogenchloride purity is 95～96%, and transport pipe nominal diameter is DN200, after concentrate, concentration of hydrochloric acid increases to 34～35%.
Described A reactor is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 886 * 6564, and heat interchanging area is 120m
2, access arrangement concentration of hydrochloric acid is 34～35%, Trimethylamine 99 purity is 99.7～99.8%, and transport pipe nominal diameter is DN50, and control pressure is at < 0.2MPa, and after concentrate, trimethylamine hydrochloride concentration increases to 57～58.6%.
Described hydrogen chloride absorption device is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 620 * 5240, and heat interchanging area is 60m
2, access arrangement Trimethylamine 99 concentration of hydrochloric acid is 57～58.6%, and transport pipe nominal diameter is DN65, and hydrogenchloride purity is 95～96%, and transport pipe nominal diameter is DN200, after absorbing, trimethylamine hydrochloride pH value reaches 1～2.
Described second reactor is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 886 * 6564, and heat interchanging area is 120m
2, access arrangement trimethylamine hydrochloride pH value 1～2, Trimethylamine 99 purity is 99.7～99.8%, and transport pipe nominal diameter is DN50, and control pressure is at < 0.2MPa, and after concentrate, trimethylamine hydrochloride concentration increases to 67～70%.
Described hydrochloric acid concentrate absorption cell, hydrogen chloride absorption groove material are glass reinforced plastic, and specification is ￠ 1350 * 2100, and volume is 3.7m
2.
Described one-tenth salt oven is jacketed lass lining enclosed reactor, housing parameter: use temperature: 100 ℃; Chuck parameter: media name: recirculated cooling water, use temperature :≤60, volume 8m
3.
Described recycle pump is magnetic drive pump, flow: 30m
3∕ h, lift: 20m.
Claims (10)
1. a device of producing trimethylamine hydrochloride, it is characterized in that: comprise hydrochloric acid concentrate resorber, hydrochloric acid concentrate absorption cell, A reactor, hydrogen chloride absorption device, hydrogen chloride absorption groove, second reactor and become salt oven, wherein, hydrochloric acid concentrate absorber bottom is connected with hydrochloric acid concentrate absorption cell top; Hydrochloric acid concentrate absorption cell bottom is connected with A reactor bottom with hydrochloric acid concentrate absorber overhead respectively, and connecting pipeline is provided with recycle pump and control valve; A reactor top is connected with hydrogen chloride absorption device top; Hydrogen chloride absorption device bottom is connected with hydrogen chloride absorption groove top; Hydrogen chloride absorption trench bottom is connected with second reactor bottom with hydrogen chloride absorption device top respectively, and connecting pipeline is provided with recycle pump and control valve; Second reactor top is connected with becoming salt oven top; Become between salt oven top and bottom and be provided with circulation line, circulation line is provided with recycle pump and trimethylamine hydrochloride finished product pipeline; Hydrochloric acid concentrate absorber overhead and hydrogen chloride absorption device top are all connected with hydrogen chloride gas pipeline; Hydrochloric acid concentrate absorber overhead is connected with hydrochloric acid pipeline; On hydrochloric acid concentrate absorption cell and hydrogen chloride absorption groove, be all connected with tail gas recycle pipeline; A reactor and second reactor bottom are all connected with Trimethylamine 99 pipeline; Described connection is pipeline and connects.
2. a kind of device of producing trimethylamine hydrochloride according to claim 1, is characterized in that: described one-tenth salt oven top is connected with hydrochloric acid pipeline and Trimethylamine 99 pipeline.
3. a kind of device of producing trimethylamine hydrochloride according to claim 1 and 2, is characterized in that: described hydrochloric acid concentrate resorber is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 620 * 5240, and heat interchanging area is 60m
2.
4. a kind of device of producing trimethylamine hydrochloride according to claim 1 and 2, is characterized in that: described A reactor is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 886 * 6564, and heat interchanging area is 120m
2.
5. a kind of device of producing trimethylamine hydrochloride according to claim 1 and 2, is characterized in that: described hydrogen chloride absorption device is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 620 * 5240, and heat interchanging area is 60m
2.
6. a kind of device of producing trimethylamine hydrochloride according to claim 1 and 2, is characterized in that: described second reactor is graphite heat exchanger, and heat-eliminating medium is recirculated water, and specification is ￠ 886 * 6564, and heat interchanging area is 120m
2.
7. a kind of device of producing trimethylamine hydrochloride according to claim 1 and 2, is characterized in that: described hydrochloric acid concentrate absorption cell, hydrogen chloride absorption groove material are glass reinforced plastic, and specification is ￠ 1350 * 2100, and volume is 3.7m
3.
8. a kind of device of producing trimethylamine hydrochloride according to claim 1 and 2, is characterized in that: described one-tenth salt oven is jacketed lass lining enclosed reactor, housing parameter: use temperature: 100 ℃; Chuck parameter: media name: recirculated cooling water, use temperature :≤60 ℃, volume 8m
3.
9. a method of producing trimethylamine hydrochloride, it is characterized in that: step is as follows: first, 31% hydrochloric acid and 95～96% hydrogenchloride are at hydrochloric acid concentrate resorber, juice circulation between hydrochloric acid concentrate absorption cell, when concentration of hydrochloric acid increases to 34～35%, enter A reactor, the Trimethylamine 99 that is 99.7～99.8% with purity reacts, reacted trimethylamine hydrochloride enters hydrogen chloride absorption device, trimethylamine hydrochloride and hydrogenchloride are at hydrogen chloride absorption device, between hydrogen chloride absorption groove, circulate, until trimethylamine hydrochloride pH value, be down to 1～2 o'clock, enter second reactor, the Trimethylamine 99 that is 99.7～99.8% with concentration reacts, after reaction, trimethylamine hydrochloride is sent into into salt oven, then trimethylamine hydrochloride is exported by trimethylamine hydrochloride finished product pipeline, the tail gas producing is sent into tail gas absorption tank by tail gas recycle pipeline and is reclaimed.
10. a kind of method of producing trimethylamine hydrochloride according to claim 9, is characterized in that: described trimethylamine hydrochloride enters into after salt oven, to becoming in salt oven to add micro-Trimethylamine 99 or/and salt acid for adjusting pH value is adjusted to pH6.5～7.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210563480.3A CN103044265B (en) | 2012-12-21 | 2012-12-21 | Device and method for producing high-concentration trimethylamine hydrochloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210563480.3A CN103044265B (en) | 2012-12-21 | 2012-12-21 | Device and method for producing high-concentration trimethylamine hydrochloride |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103044265A CN103044265A (en) | 2013-04-17 |
| CN103044265B true CN103044265B (en) | 2014-04-23 |
Family
ID=48057152
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210563480.3A Expired - Fee Related CN103044265B (en) | 2012-12-21 | 2012-12-21 | Device and method for producing high-concentration trimethylamine hydrochloride |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103044265B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106560467A (en) * | 2016-06-27 | 2017-04-12 | 宁夏海诚电化信息科技有限公司 | Trimethylamine hydrochloride production process |
| CN115636751A (en) * | 2022-06-14 | 2023-01-24 | 山东一飞药业股份有限公司 | Production process of trimethylamine hydrochloride |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2115094B2 (en) * | 1971-03-29 | 1981-07-23 | Basf Ag, 6700 Ludwigshafen | Process for the continuous production of an aqueous choline chloride solution |
| DD241595B1 (en) * | 1985-10-04 | 1990-06-20 | Chemisch Pharmazeutisches Werk | METHOD AND DEVICE FOR PREPARING CHOLIN CHLORIDE |
| CN101691333B (en) * | 2009-10-21 | 2012-07-25 | 山东恩贝科技有限公司 | Production technology for choline chloride |
-
2012
- 2012-12-21 CN CN201210563480.3A patent/CN103044265B/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN103044265A (en) | 2013-04-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109879258B (en) | Device and method for preparing nitric acid by efficiently oxidizing and absorbing nitrogen oxides | |
| CN103044265B (en) | Device and method for producing high-concentration trimethylamine hydrochloride | |
| CN106010649A (en) | Chlorinated paraffin continuous production process efficiently utilizing chlorine gas | |
| CN105063108A (en) | Enhancing method for producing malic acid through biological electrodialysis | |
| CN111606867B (en) | Device and method for coproducing melamine by using differentiated urea | |
| CN203857828U (en) | Exhaust heat recovery system of vanadium-nitrogen alloy production kiln | |
| CN105237357B (en) | A kind of hydrogenation reaction device | |
| CN206626848U (en) | One kind utilizes second-kind absorption-type heat pump recovery waste heat system | |
| CN221245139U (en) | Carbonization tower for producing nano active calcium carbonate | |
| CN203382694U (en) | Nitration reaction device | |
| CN217725090U (en) | Ammonia recycling system | |
| CN207734641U (en) | A kind of crystallizing tank of energy uniform decrease in temperature | |
| CN219377088U (en) | Energy-saving production device for polyamide polyamine epichlorohydrin | |
| CN205115336U (en) | Hydrogenation device | |
| CN203295398U (en) | Circulating device for preparing urea | |
| CN203033916U (en) | Heat utilization system of cyclohexane device reactor | |
| CN203498103U (en) | White carbon black thin pulp circulation type heat-exchange preparation system | |
| CN115463519B (en) | Method and system for producing nitrososulfuric acid with high efficiency | |
| CN104763486B (en) | Formaldehyde method for power generation by waste heat and generator set thereof | |
| CN212388001U (en) | Low-temperature heat recycling system of hydrogen adding device | |
| CN210710749U (en) | S03Device for recovering waste heat of absorbing sulfuric acid | |
| CN202204132U (en) | Device for heating water by recycling heat of polycrystalline silicon reduction furnace | |
| CN204824678U (en) | Adopt device of downstream process production sodium formate | |
| CN219815305U (en) | Dimethyl ether condensate heat cascade utilization device | |
| CN203750528U (en) | Circulation cooling device for reaction kettle |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140423 Termination date: 20151221 |
|
| EXPY | Termination of patent right or utility model |