CN108329323A - A method of continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction - Google Patents
A method of continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction Download PDFInfo
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- CN108329323A CN108329323A CN201710041165.7A CN201710041165A CN108329323A CN 108329323 A CN108329323 A CN 108329323A CN 201710041165 A CN201710041165 A CN 201710041165A CN 108329323 A CN108329323 A CN 108329323A
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- ammonia
- formaldehyde
- tower
- absorbing tower
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- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 title claims abstract description 171
- VKYKSIONXSXAKP-UHFFFAOYSA-N hexamethylenetetramine Chemical compound C1N(C2)CN3CN1CN2C3 VKYKSIONXSXAKP-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000007788 liquid Substances 0.000 title claims abstract description 27
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 134
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 65
- 238000010521 absorption reaction Methods 0.000 claims abstract description 21
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 235000010299 hexamethylene tetramine Nutrition 0.000 claims abstract description 15
- 229960004011 methenamine Drugs 0.000 claims abstract description 15
- 239000012452 mother liquor Substances 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000001914 filtration Methods 0.000 claims abstract description 7
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 40
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000002425 crystallisation Methods 0.000 abstract 1
- 230000008025 crystallization Effects 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 238000012856 packing Methods 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- 239000000908 ammonium hydroxide Substances 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- XQJMXPAEFMWDOZ-UHFFFAOYSA-N 3exo-benzoyloxy-tropane Natural products CN1C(C2)CCC1CC2OC(=O)C1=CC=CC=C1 XQJMXPAEFMWDOZ-UHFFFAOYSA-N 0.000 description 1
- QQXLDOJGLXJCSE-UHFFFAOYSA-N N-methylnortropinone Natural products C1C(=O)CC2CCC1N2C QQXLDOJGLXJCSE-UHFFFAOYSA-N 0.000 description 1
- QIZDQFOVGFDBKW-DHBOJHSNSA-N Pseudotropine Natural products OC1C[C@@H]2[N+](C)[C@H](C1)CC2 QIZDQFOVGFDBKW-DHBOJHSNSA-N 0.000 description 1
- 241000009298 Trigla lyra Species 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- -1 pressure Chemical compound 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- CYHOMWAPJJPNMW-JIGDXULJSA-N tropine Chemical compound C1[C@@H](O)C[C@H]2CC[C@@H]1N2C CYHOMWAPJJPNMW-JIGDXULJSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D487/00—Heterocyclic compounds containing nitrogen atoms as the only ring hetero atoms in the condensed system, not provided for by groups C07D451/00 - C07D477/00
- C07D487/12—Heterocyclic compounds containing nitrogen atoms as the only ring hetero atoms in the condensed system, not provided for by groups C07D451/00 - C07D477/00 in which the condensed system contains three hetero rings
- C07D487/18—Bridged systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/58—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of methods continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction, and ammonia tail gas is imported formaldehyde absorbing tower, is handled ammonia tail gas, is as follows：Ammonia after filtering is passed through formaldehyde absorbing tower, is configured to ammonia spirit；Above-mentioned ammonia spirit is subjected to tower cycle, then is passed through gas formaldehyde, tower temperature rises rapidly, carries out reaction and generates 20 ~ 35% Urotropine mother liquid of content；Mother liquor is entered into methenamine device ammoniation reactor, control temperature, pH value and vacuum degree after metering；Continuous concentration or batch concentration are discarded to mother liquor crystallization slot to mother liquor content 38 ~ 42% in ammoniation reactor reactor.The method of the present invention, chemical reaction absorption is carried out in the case where not increasing any power cost using formaldehyde absorbing tower circulating pump, efficient, adjustment is flexible and convenient, and the reaction heat in reactor is advantageously reduced, and recirculated water can be saved, meet the industrial policy of the energy-saving environmental protection in China.
Description
Technical field
The present invention relates to industrial tail gas recovery technology fields more particularly to a kind of utilization formaldehyde absorbing tower coproduction continuously to prepare
The method of Urotropine mother liquid.
Background technology
In current domestic urotropine by using gas phase method production technology, traditional urotropine by using gas phase method production technology is by gas
Body formaldehyde and ammonia carry out being condensed in alkaline solution（Specific flow chart is referring to Fig. 1）.In the actual production process, existing
Urotropine by using gas phase method production technology be methanol it is inverted after generate formaldehyde gas, be passed directly into ammoniation reactor with
Ammonia reaction generates Urotropine mother liquid.But urotropine by using gas phase method production process route is short, reactor when especially device proposes production
The interior high cycle speed reaction time is short, be easy to cause incomplete reaction, and product purity is not high, can also cause in reactor liquid fluctuating and
Pressure fluctuation, the serious phenomenon of gas entrainment.In order to make reaction be carried out to methenamine direction is generated, while avoiding pair
Reaction generates and influences product quality and consumption of raw materials, therefore stringent controlling reaction temperature and ensures ammonia excessive 1% ~ 2%.From reaction
Inert gas, vapor and the ammonia that does not react completely that device comes out pass through ammonia absorber, and most ammonia and vapor are followed
Ring liquid absorbs the ammonia not absorbed into ammonium hydroxide liquid seal trough and inert gas after gas cooler by vacuum pumping
Enter tail gas boiler combustion.
Invention content
Technical problems based on background technology, the present invention, which proposes, a kind of continuously to be prepared using formaldehyde absorbing tower coproduction
The method of Urotropine mother liquid, project of the present invention are to establish to prepare unsaturation Wu Luotuo using the transformation of existing formaldehyde plant absorption tower
Product mother liquor reactor makes existing production capacity increase, and reaction is abundant, and consumption reduces, and reduces cost, improves the market competitiveness and reduces dirt
Dye.
Technical scheme is as follows：
A method of Urotropine mother liquid continuously being prepared using formaldehyde absorbing tower coproduction, ammonia tail gas is imported into formaldehyde absorption
Tower handles ammonia tail gas, is as follows：
（1）It will be passed through formaldehyde absorption tower bottom distributor after ammonia metering after filtering, is dispersed in demineralized water, is configured to PH
7.5 ~ 9.0 ammonia spirit of value；
（2）Above-mentioned ammonia spirit is subjected to tower cycle, then is passed through gas formaldehyde, tower temperature rises rapidly, and control tower temperature is 50~85
DEG C, pH value control 8.0 ~ 9.5 carries out reaction and generates 20 ~ 35% Urotropine mother liquid of content；
（3）By mother liquor after metering enter methenamine device ammoniation reactor, control ammoniation reactor temperature at 75 ~ 95 DEG C,
PH value 7.5 ~ 9.0, vacuum degree control are -10 ~ -25kpa；
（4）Continuous concentration or batch concentration are discarded to methenamine to mother liquor content 38 ~ 42% in ammoniation reactor reactor
Crystallize groove.
Ammonia comes from liquid ammonia evaporator：Ammonia needed for reaction comes from liquid ammonia evaporator, and liquefied ammonia evaporates in ammonia evaporator,
Constant pressure then is reduced to, the ammonia of generation enters reactor ammonia relevant parameters after filtering, by metering with control piper
Such as pressure, temperature and component etc., which have to comply with, requires to meet the following conditions:
Ammonia content, % >=99.6
Residuals content, %≤0.4
Oil content, mg/kg≤5 (gravimetric method) 2 (infra-red sepectrometry)
Temperature≤80 DEG C
Pressure >=20 ~ 100KPa.
Preferably, the step（2）In, excess ammonia is controlled 0.5 ~ 1.5%.
The manufacturing technique of the present invention are as follows coproduction project, which continuously prepares methenamine mother using formaldehyde absorbing tower coproduction
The method of liquid is connected to formaldehyde absorbing tower using existing section of tubing and carries out water absorption or reactive absorption again, wherein spare
Mouth goes to incinerator.
Wherein formaldehyde plant of the gas formaldehyde body from joint workshop section.The relevant parameter of gas formaldehyde such as pressure, temperature and
Component etc., which has to comply with, requires in general, and gas formaldehyde, which enters formaldehyde absorbing tower, should meet the following conditions:
Temperature: 90~110℃
Pressure: 2~10KPa
Content of formaldehyde: 22.124 %
Methanol content: 0.478%
Water content: 19.75%
Hydrogen content: 0.7394%
CO2Content: 4.132%
N2Content: 52.328%
The invention has the beneficial effects that：The method of the present invention is inhaled in the case where not increasing any power cost using formaldehyde
It receives tower circulating pump and carries out chemical reaction absorption, efficient, adjustment is flexible and convenient, can recycle ammonium hydroxide, and be conducive to subtract
Reaction heat in few reactor, and recirculated water can be saved, meet the industrial policy of the energy-saving environmental protection in China.The black Lip river of the present invention
The absorption of free ammonia in tropine production line emission, can reduce by 20 ~ 25Kg of methenamine ammonia unit consumption per ton.To produce 20000 tons per year
It calculates, can at most save 400 tons of liquefied ammonia, calculated by 2000 yuan per ton, more than 80 ten thousand yuan of production cost can be saved every year, be enterprise's band
Huge economic benefit and environmentally friendly social benefit are come.
Specific implementation mode
Fig. 1 is traditional urotropine by using gas phase method production technological process.
Fig. 2 is excessive ammonia recycling process diagram in the tail gas of the present invention.
Specific implementation mode
Embodiment 1：
A method of Urotropine mother liquid continuously being prepared using formaldehyde absorbing tower coproduction, ammonia tail gas is imported into formaldehyde absorption
Tower handles ammonia tail gas, is as follows：
（1）It will be passed through formaldehyde absorption tower bottom distributor after ammonia metering after filtering, is dispersed in demineralized water, is configured to PH
8.0 ammonia spirit of value；
（2）Above-mentioned ammonia spirit is subjected to tower cycle, then is passed through gas formaldehyde, tower temperature rises rapidly, and control tower temperature is at 75 DEG C, PH
Value control 8.5 carries out reaction and generates 25% Urotropine mother liquid of content；
（3）Mother liquor is entered into methenamine device ammoniation reactor after metering, control ammoniation reactor temperature is at 85 DEG C, pH value
8.5, vacuum degree control is -20kpa；
（4）Continuous concentration or batch concentration are discarded to methenamine knot to mother liquor content 40% in ammoniation reactor reactor
Brilliant groove.
The step（1）In, when ammonia enters formaldehyde absorbing tower, condition is as follows:
Ammonia content, 99.8%
Residuals content, 0.2%
Oil content ,≤3.5mg/kg (gravimetric method)
Temperature, 70 DEG C
Pressure, 55KPa.
The step（2）In, excess ammonia is controlled 1.0%.
The step（2）In, when gas formaldehyde enters formaldehyde absorbing tower, condition is as follows:
Temperature: 95℃
Pressure: 8KPa
Content of formaldehyde: 22.124 %
Methanol content: 0.478%
Water content: 19.75%
Hydrogen content: 0.7394%
CO2Content: 4.132%
N2Content: 52.328%.
Embodiment 2：
A method of Urotropine mother liquid continuously being prepared using formaldehyde absorbing tower coproduction, ammonia tail gas is imported into formaldehyde absorption
Tower handles ammonia tail gas, is as follows：
（1）It will be passed through formaldehyde absorption tower bottom distributor after ammonia metering after filtering, is dispersed in demineralized water, is configured to PH
9.0 ammonia spirit of value；
（2）Above-mentioned ammonia spirit is subjected to tower cycle, then is passed through gas formaldehyde, tower temperature rises rapidly, and control tower temperature is at 50 DEG C, PH
Value control 9.5 carries out reaction and generates 20% Urotropine mother liquid of content；
（3）Mother liquor is entered into methenamine device ammoniation reactor after metering, control ammoniation reactor temperature is at 95 DEG C, pH value
7.5, vacuum degree control is -25kpa；
（4）Continuous concentration or batch concentration are discarded to methenamine knot to mother liquor content 38% in ammoniation reactor reactor
Brilliant groove.
The step（1）In, when ammonia enters formaldehyde absorbing tower, condition is as follows:
Ammonia content, 99.7%
Residuals content, 0.3%
Oil content ,≤1.8mg/kg (infra-red sepectrometry)
Temperature, 80 DEG C
Pressure, 25KPa.
The step（2）In, excess ammonia is controlled 0.5%.
The step（2）In, when gas formaldehyde enters formaldehyde absorbing tower, condition is as follows:
Temperature: 110℃
Pressure: 2KPa
Content of formaldehyde: 25%
Methanol content: 0.4%
Water content: 21%
Hydrogen content: 0.7%
CO2Content: 5%
N2Content: 55%.
Embodiment 3：
A method of Urotropine mother liquid continuously being prepared using formaldehyde absorbing tower coproduction, ammonia tail gas is imported into formaldehyde absorption
Tower handles ammonia tail gas, is as follows：
（1）It will be passed through formaldehyde absorption tower bottom distributor after ammonia metering after filtering, is dispersed in demineralized water, is configured to PH
7.5 ammonia spirit of value；
（2）Above-mentioned ammonia spirit is subjected to tower cycle, then is passed through gas formaldehyde, tower temperature rises rapidly, and control tower temperature is at 85 DEG C, PH
Value control 8.0 carries out reaction and generates 35% Urotropine mother liquid of content；
（3）Mother liquor is entered into methenamine device ammoniation reactor after metering, control ammoniation reactor temperature is at 75 DEG C, pH value
9.0, vacuum degree control is -10kpa；
（4）Continuous concentration or batch concentration are discarded to methenamine knot to mother liquor content 42% in ammoniation reactor reactor
Brilliant groove.
The step（1）In, when ammonia enters formaldehyde absorbing tower, condition is as follows:
Ammonia content, 99.6%
Residuals content, 0.4%
Oil content ,≤1.5mg/kg (infra-red sepectrometry)
Temperature, 60 DEG C
Pressure, 100KPa.
The step（2）In, excess ammonia is controlled 1.5%.
The step（2）In, when gas formaldehyde enters formaldehyde absorbing tower, condition is as follows:
Temperature: 90℃
Pressure: 10KPa
Content of formaldehyde: 22%
Methanol content: 0.5%
Water content: 18%
Hydrogen content: 1.0%
CO2Content: 4%
N2Content: 55%.
The operation principle of the present invention：
Absorption operation is carried out using formaldehyde absorbing tower, is that can generally reach 2m or more because formaldehyde absorbing tower diameter is huge, this
Sample can provide huge gas-liquid mass transfer area and filler surface has good turbulent flow conditions.Ammonia air inlet below the tower body
Mouth is full of air inlet section space, then rises to first order packing material absorbing section uniformly across flow equalization section tangentially into absorption tower.
On the surface of filler, ammonia is chemically reacted with water in liquid phase or formaldehyde in gas phase, and the absorption process of ammonia is predominantly changed
It learns and absorbs, mother liquor controls always carries out condensation reaction generation methenamine and water in undersaturated condition formalin and ammonia,
And release heat.
Reaction equation： 6 CH2O（Liquid）+ 4 NH3（Gas）→ (CH2)6N4 + 6 H2O
The ammonia gas not fully absorbed continues to ascend into second level spray section.Then ammonia rises to two level packing section, spray
Absorption process similar with the first order Duan Jinhang.The second level and first order absorption gas concentration range are also different.It is spraying
The process that section and packing section two are in contact is also the process of heat and mass transfer.Ensure this by control tower flow velocity and residence time
The abundant and stabilization of process.The topmost of tower body is demisting section, and folded absorbing liquid droplet is eliminated herein in gas,
Tail gas after treatment has been the air of more cleaning, it is discharged into tail gas boiler from absorption tower upper end discharge duct.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto,
Any one skilled in the art in the technical scope disclosed by the present invention, according to the technique and scheme of the present invention and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (4)
1. a kind of method continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction, which is characterized in that by ammonia tail gas
Formaldehyde absorbing tower is imported, ammonia tail gas is handled, is as follows：
（1）It will be passed through formaldehyde absorption tower bottom distributor after ammonia metering after filtering, is dispersed in demineralized water, is configured to PH
7.5 ~ 9.0 ammonia spirit of value；
（2）Above-mentioned ammonia spirit is subjected to tower cycle, then is passed through gas formaldehyde, tower temperature rises rapidly, and control tower temperature is 50~85
DEG C, pH value control 8.0 ~ 9.5 carries out reaction and generates 20 ~ 35% Urotropine mother liquid of content；
（3）By mother liquor after metering enter methenamine device ammoniation reactor, control ammoniation reactor temperature at 75 ~ 95 DEG C,
PH value 7.5 ~ 9.0, vacuum degree control are -10 ~ -25kpa；
（4）Continuous concentration or batch concentration are discarded to methenamine to mother liquor content 38 ~ 42% in ammoniation reactor reactor
Crystallize groove.
2. the method for continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction as described in claim 1, feature exist
In the step（1）In, when ammonia enters formaldehyde absorbing tower, condition is as follows:
Ammonia content, % >=99.6
Residuals content, %≤0.4
Oil content, mg/kg≤5 (gravimetric method) or oil content, mg/kg≤2 (infra-red sepectrometry)
Temperature≤80 DEG C
Pressure >=20 ~ 100KPa.
3. the method for continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction as described in claim 1, feature exist
In the step（2）In, when gas formaldehyde enters formaldehyde absorbing tower, condition is as follows:
Temperature: 90~110℃
Pressure: 2~10KPa
Content of formaldehyde: 22~25%
Methanol content: 0.2~1.0%
Water content: 18~21%
Hydrogen content: 0.7~1.0%
CO2Content: 4~5%
N2Content: 50~55%.
4. the method for continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction as described in claim 1, feature exist
In the step（2）In, excess ammonia is controlled 0.5 ~ 1.5%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710041165.7A CN108329323A (en) | 2017-01-20 | 2017-01-20 | A method of continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710041165.7A CN108329323A (en) | 2017-01-20 | 2017-01-20 | A method of continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108329323A true CN108329323A (en) | 2018-07-27 |
Family
ID=62922700
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710041165.7A Pending CN108329323A (en) | 2017-01-20 | 2017-01-20 | A method of continuously preparing Urotropine mother liquid using formaldehyde absorbing tower coproduction |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110883311A (en) * | 2019-12-31 | 2020-03-17 | 重庆长江造型材料（集团）股份有限公司 | Modification method of urotropine |
| CN112354487A (en) * | 2020-11-06 | 2021-02-12 | 李东田 | Preparation method of ammonium carbonate feed gas |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4198332A (en) * | 1978-10-06 | 1980-04-15 | Th. Goldschmidt Ag | Process for the preparation of solutions of urea-formaldehyde resins for the impregnation and coating of carrier webs for coating the surface of wood-based panels |
| CN101045847A (en) * | 2006-03-31 | 2007-10-03 | 中国科学院过程工程研究所 | Adhesive and paint for absorbing formol |
| CN102398996A (en) * | 2010-09-09 | 2012-04-04 | 孙波 | Scale remover for boiler water processing equipment |
| CN203187610U (en) * | 2013-04-26 | 2013-09-11 | 山西阳煤丰喜肥业(集团)有限责任公司 | Methenamine production device |
| CN204918230U (en) * | 2015-06-23 | 2015-12-30 | 浙江南化防腐设备有限公司 | Ammonia nitrogen blows and takes off, absorbs synthetic urotropine equipment |
-
2017
- 2017-01-20 CN CN201710041165.7A patent/CN108329323A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4198332A (en) * | 1978-10-06 | 1980-04-15 | Th. Goldschmidt Ag | Process for the preparation of solutions of urea-formaldehyde resins for the impregnation and coating of carrier webs for coating the surface of wood-based panels |
| CN101045847A (en) * | 2006-03-31 | 2007-10-03 | 中国科学院过程工程研究所 | Adhesive and paint for absorbing formol |
| CN102398996A (en) * | 2010-09-09 | 2012-04-04 | 孙波 | Scale remover for boiler water processing equipment |
| CN203187610U (en) * | 2013-04-26 | 2013-09-11 | 山西阳煤丰喜肥业(集团)有限责任公司 | Methenamine production device |
| CN204918230U (en) * | 2015-06-23 | 2015-12-30 | 浙江南化防腐设备有限公司 | Ammonia nitrogen blows and takes off, absorbs synthetic urotropine equipment |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110883311A (en) * | 2019-12-31 | 2020-03-17 | 重庆长江造型材料（集团）股份有限公司 | Modification method of urotropine |
| CN112354487A (en) * | 2020-11-06 | 2021-02-12 | 李东田 | Preparation method of ammonium carbonate feed gas |
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Application publication date: 20180727 |
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