CN206654738U - Methanol and ammonium chloride extraction equipment in a kind of glycine production - Google Patents
Methanol and ammonium chloride extraction equipment in a kind of glycine production Download PDFInfo
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- CN206654738U CN206654738U CN201720307079.1U CN201720307079U CN206654738U CN 206654738 U CN206654738 U CN 206654738U CN 201720307079 U CN201720307079 U CN 201720307079U CN 206654738 U CN206654738 U CN 206654738U
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 246
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 title claims abstract description 67
- DHMQDGOQFOQNFH-UHFFFAOYSA-N Glycine Chemical compound NCC(O)=O DHMQDGOQFOQNFH-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 235000019270 ammonium chloride Nutrition 0.000 title claims abstract description 31
- 239000004471 Glycine Substances 0.000 title claims abstract description 25
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 18
- 238000000605 extraction Methods 0.000 title claims abstract description 13
- 230000000694 effects Effects 0.000 claims abstract description 125
- 239000012452 mother liquor Substances 0.000 claims abstract description 28
- 239000002562 thickening agent Substances 0.000 claims abstract description 12
- 239000000463 material Substances 0.000 claims abstract description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 15
- 239000007788 liquid Substances 0.000 abstract description 11
- 238000011084 recovery Methods 0.000 abstract description 11
- 229960002449 glycine Drugs 0.000 description 20
- 238000001704 evaporation Methods 0.000 description 11
- 230000008020 evaporation Effects 0.000 description 11
- 239000000243 solution Substances 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 5
- 238000005119 centrifugation Methods 0.000 description 5
- 238000002425 crystallisation Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000008025 crystallization Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 235000010299 hexamethylene tetramine Nutrition 0.000 description 3
- VKYKSIONXSXAKP-UHFFFAOYSA-N hexamethylenetetramine Chemical compound C1N(C2)CN3CN1CN2C3 VKYKSIONXSXAKP-UHFFFAOYSA-N 0.000 description 3
- 229960004011 methenamine Drugs 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 235000013905 glycine and its sodium salt Nutrition 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- NGNBDVOYPDDBFK-UHFFFAOYSA-N 2-[2,4-di(pentan-2-yl)phenoxy]acetyl chloride Chemical class CCCC(C)C1=CC=C(OCC(Cl)=O)C(C(C)CCC)=C1 NGNBDVOYPDDBFK-UHFFFAOYSA-N 0.000 description 1
- UKHBMLYYHZJJLS-UHFFFAOYSA-N 2-aminoacetic acid;methanol Chemical compound OC.NCC(O)=O UKHBMLYYHZJJLS-UHFFFAOYSA-N 0.000 description 1
- FWPVTRYPFNDICZ-UHFFFAOYSA-N 2-aminoethaneperoxoic acid Chemical compound NCC(=O)OO FWPVTRYPFNDICZ-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 238000007098 aminolysis reaction Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- FOCAUTSVDIKZOP-UHFFFAOYSA-N chloroacetic acid Chemical compound OC(=O)CCl FOCAUTSVDIKZOP-UHFFFAOYSA-N 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000003808 methanol extraction Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
It the utility model is related to Methanol Recovery and ammonium chloride extraction equipment in a kind of glycine production.Specific conveying pipeline is connected through feed pump with preheater, it is connected at the top of preheater with I effects heater A, I is imitated heater A and is connected with I effect evaporators, and I is imitated base of evaporator and is connected with I effects heater B, and I imitates heater B bottoms and is connected to form circulation with I effects heater A through circulating pump；I effect heater A, I effects heater B bottoms are connected through conveying pipeline with methanol discharge tank；I effect base of evaporators are connected through conveying pipeline with turning batch can, are turned batch can and are connected through transfering material pump with II effect heaters, II is imitated heater and is connected with II effect evaporators；II effect base of evaporators are connected with thickener, and thickener is connected with mother liquor pond again after being connected with centrifuge.The process steam utilization rate carried out using the equipment is high, and equipment investment is small, and mother liquid disposal is innoxious, energy-conserving and environment-protective, is adapted to extensive use in glycine industry.
Description
Technical field
The utility model belongs to glycine production technical field, more particularly to a kind of glycine produce in Methanol Recovery and
Ammonium chloride novel technology for extracting.
Background technology
Currently, amino acetic acid in China production still uses more traditional Chloroacetic Aminolysis.Due to the sweet ammonia in the Synthesis liquid
Acid and ammonium chloride different solubility in methyl alcohol, using methanol extraction, centrifuge glycine after, obtained centrifuge mother liquor contains
Substantial amounts of methanol, ammonium chloride and water, simultaneously containing a small amount of glycine, methenamine and molecules of ammonia.Because the centrifuge mother liquor is deposited
Organic matter and inorganic matter mixing, pollutant kind is more, ammonia-nitrogen content is big, methenamine high temperature easily decomposes the features such as, therefore, one
Straight the problem of annoying amino acetic acid in China enterprise：The methanol and ammonium chloride in centrifuge mother liquor are how effectively extracted, is thoroughly reached clear
Clean production.Methanol and ammonium chloride are currently reclaimed from centrifuge mother liquor mainly three big difficult points：(1) energy consumption problem；(2) equipment corrosion
Problem；(3) distillation of ammonium chloride in evaporation process be present, catalyst methenamine decomposes, high temperature evaporation causes complicated chemical anti-
The problems such as answering can produce high ammonia nitrogen, high COD evaporation condensed water and centrifugal filtrate, environmentally friendly risk be present.
Publication No. CN103303942A, entitled " a kind of method and apparatus that ammonium chloride is reclaimed from glycin mother liquid "
Utility model patent, mainly the mother liquor after the analysis of glycine alcohol, centrifugation is first passed through stuffing rectification column and isolates 90~93%
Methanol, rectifying column raffinate again by the low temperature of the two-stage countercurrent evaporator under vacuum state and flash vessel concentration after, then will
Concentrate carries out continuous cooling crystallization, finally thickens crystal solution, is centrifugally separating to obtain ammonium chloride product.But this method is deposited
Equipment requirement is high, steam energy consumption is big, product purity is low, environmental problem caused by evaporation condensed water and final mother liquor is still present
The shortcomings of.
Publication No. CN104310427A, entitled " recovery of mother liquor is sharp during a kind of chloroactic acid method production glycine
With technique " patent of invention, burn temperature by being concentrated, being burned to glycin mother liquid and crystallization treatment, and using specific
Degree and crystallization temperature, ammonium chloride loss is small, and ammonia nitrogen recovery rate is up to more than 95%, and ammonium chloride quality is high, and mother liquor is up to harmless
Change is handled.But incineration temperature needs 700~1000 DEG C and crystallization temperature to need 300 DEG C, it is larger to heat fuel used energy consumption,
Operating cost is higher.
The content of the invention
In order to overcome the above-mentioned deficiencies of the prior art, the utility model provide in a kind of production of glycine Methanol Recovery and
Ammonium chloride novel technology for extracting, reach energy-saving, mother liquor harmless treatment, reduce equipment failure rate, reduce maintenance and run into
Originally, thoroughly solves environmental issue.
The utility model by lobed rotor compressor effect mainly by the glycin mother liquid containing methanol and ammonium chloride by being provided
The economic benefits and social benefits low-temperature evaporation concentration systems of thermal source, through the isolated ammonium chloride of continuous crystallisation, while it can connect without being related to rectifier unit
Continuous recovery methanol solution, comprises the following steps：
Methanol and ammonium chloride extraction equipment in a kind of glycine production, conveying pipeline are connected with preheater through feed pump, preheated
It is connected at the top of device with I effects heater A, I is imitated heater A and is connected with I effect evaporators, and I effect base of evaporators connect with I effect heaters B
Connect, I imitates heater B bottoms and is connected to form circulation with I effects heater A through circulating pump；
I effect heater A, I effects heater B bottoms are connected through conveying pipeline with methanol discharge tank；
I effect base of evaporators are connected through conveying pipeline with turning batch can, are turned batch can and are connected through transfering material pump with II effect heaters, II effects
Heater is connected with II effect evaporators；
II effect base of evaporators are connected with thickener, and thickener is connected with mother liquor pond again after being connected with centrifuge.
It is connected at the top of described I effect evaporators with I effect Roots's methanol compressors, I effect Roots's methanol compressors exist through oxygen
Line analysis instrument is connected with I effect heater A, I effects heater B respectively, and methanol discharge tank imitates Roots's methanol pressure through methanol discharging pump and I
Contracting machine connects, and forms circulating system.
Described II effects evaporator bottom is connected through conveying pipeline with forced circulation pump, and forced circulation pump connects with II effect heaters
Connect, II is imitated heater and is connected with II effect evaporators；Described mother liquor pond is connected through mother liquor reflux pump with forced circulation pump.
The connection of Roots's methanol compressor is imitated through II at the top of described II effect evaporators, II effect Roots's methanol compressors are divided to two
Road, it is connected with I effect heater A, I effects heater B, is connected all the way with condenser respectively all the way, condenser is connected with dilute methanol tank,
Methanol discharge tank is connected through methanol discharging pump with II effect Roots's methanol compressors, forms circulating system.
Methanol and ammonium chloride extracting method in a kind of glycine production, comprise the following steps：
(1) raw steam first is passed through into II effect heater, adjusts steam flow, control preheater temperature.
(2) centrifuge the mother liquor after glycine and be heated to 30~40 DEG C by preheater, heat source medium secondary use II
Imitate the latent heat of condensed water caused by raw steam in heater.
(3) preheating material concentrates system by the flush distillation being made up of I effect heater A, I effect evaporator and I effect heater B
System, the interior holding vacuum of system is -0.07Mpa.
(4) methanol solution is gasificated into the methanol steam of about 50~60 DEG C of temperature in I effect evaporator under vacuum condition, utilizes
I effect Roots's methanol compressor makes methanol steam bring up to 60~70 DEG C, and the methanol steam after temperature raising enters to be heated into I effect side by side
The effect heaters of device A and I B shell side carries out secondary use.This system monitors oxygen content in real time with oxygen in-line analyzer, prevent be
Nitrogen displacement of uniting is not thorough or air enters in the process of running, causes the exceeded generation security incident of system oxygen content.
(5) I effect heater A and I effect heater B shell side condensate liquid can be configured to 92% or so methanol solution, centrifugation
The methanol solution of 90% volume is efficiently separated in mother liquor after separation of glycine.
(6) solution containing a large amount of ammonium chlorides evaporates from I effect base of evaporator extraction into by II effect heater and II effect
The double evaporation-cooling concentration systems of device composition, the interior holding vacuum of system are -0.07Mpa, and II effect heater is using raw steam offer
Original heat source.
(7) aqueous solution of methanol is vaporized into the first alcohol and water of about 80~85 DEG C of temperature in II effect evaporator under vacuum condition
Mixed vapour, using II effect Roots's methanol compressor methanol steam is brought up to 90~95 DEG C, the methanol steam one after temperature raising
Part enters I effect heater A side by side and I effect heater B shell side carries out secondary use, as heat supplement, is partly into
Condenser, which condenses to obtain, washes methanol solution.So far, methanol, water are efficiently separated from the mother liquor after centrifugation glycine.
After about 80 DEG C of saturated ammonium chloride solutions are thickened into thickener in (8) II effect evaporators, feed liquid be put into from
Ammonium chloride product is isolated in scheming.So far, glycine centrifuge mother liquor is effectively addressed.
In above-mentioned system, temperature, pressure system are as follows：
Currently, the mother liquid disposal after glycine industry centrifuges for glycine, is generally first isolated using rectifying column
Methanol, rectifying column raffinate is then subjected to economic benefits and social benefits low-temperature evaporation recovery ammonium chloride.In contrast to this, this method has the following advantages：
(1) whole process steam utilization is higher, and steam energy consumption is relatively low, and the initial II effect heater temperature rise period of only driving needs
Steam is largely given birth to, miscellaneous equipment provides thermal source using material steam.
(2) system is not related to large-scale rectifying tower, equipment investment is smaller to the less demanding of equipment and pipeline.
(3) methanol concentration can accurately be adjusted according to needs of production.
(4) oxygen in-line analyzer monitors oxygen content in real time, and anti-locking system nitrogen displacement is not thorough or in the process of running
Air enters, and safety coefficient is high.
(5) mother liquor can reach harmless treatment, will not produce high ammonia nitrogen, high COD plain boiled water, will not also produce ammonium chloride
Red waste water after separation, can reach green production.
(6) due in system evaporation process temperature be less than 80 DEG C, complex reaction will not occur between organic matter, feed liquid
COD, colourity, viscosity will not be significantly increased, and intractability is little.
(7) purity of ammonia chloride height, the quality better of this technique recovery, can reach the white crystal of technical grade, can increase warp
Ji benefit.
(8) this technique has that technique, equipment are simple, easy to operate.
Brief description of the drawings
Fig. 1 is methanol and ammonium chloride extraction equipment structure chart in glycine production, wherein, 1. feed pumps, 2. preheaters,
3.I effect heater A, 4.I effect heater B, 5.I effect evaporators, 6.I effect Roots's methanol compressors, 7. oxygen in-line analyzers, 8.
Methanol discharge tank, 9. circulating pumps, 10. dilute methanol tanks, 11. turns of batch cans, 12. condensers, 13. transfering material pumps, 14.II effect heaters,
15.II effect evaporators, 16.II effect Roots's methanol compressors, 17. forced circulation pumps, 18. mother liquor reflux pumps, 19. mother liquor ponds,
20. thickener, 21. centrifuges.
Embodiment
New technology recovery methanol, the specific implementation step of ammonium chloride are as follows：
Embodiment 1
Raw steam is passed through into II effect heater, regulation steam flow causes preheater temperature to reach 40 DEG C；By glycine
Mother liquor after centrifugation is slowly introducing preheater so that temperature of charge reaches 40 DEG C；Preheating material enters by I effect heater A, I effect
The one-level evaporation concentration system of evaporator and I effect heater B compositions, I effect evaporator top vacuum holding -0.07Mpa, temperature
60 DEG C are maintained, temperature is 70 DEG C after I effect Roots's methanol compressor；It is passed through from the material of I effect base of evaporator extraction by II effect
The double evaporation-cooling concentration systems of heater and II effect evaporator composition, II effect evaporator top vacuum holding -0.07Mpa, temperature
Degree maintains 85 DEG C, and temperature is 95 DEG C after II effect Roots's methanol compressor；During dual evaporation, methanol constantly produces, concentration
About 90~95%；After about 80 DEG C of saturated ammonium chloride solution is thickened into thickener in II effect evaporator, feed liquid is put into
Centrifuge isolates white ammonium chloride product, purity of ammonia chloride 99.5%, ammonia nitrogen recovery rate more than 98%.
Embodiment 2
Raw steam is passed through into II effect heater, regulation steam flow causes preheater temperature to reach 40 DEG C；By glycine
Mother liquor after centrifugation is slowly introducing preheater so that temperature of charge reaches 40 DEG C；Preheating material enters by I effect heater A, I effect
The one-level evaporation concentration system of evaporator and I effect heater B compositions, I effect evaporator top vacuum holding -0.08Mpa, temperature
50 DEG C are maintained, temperature is 60 DEG C after I effect Roots's methanol compressor；It is passed through from the material of I effect base of evaporator extraction by II effect
The double evaporation-cooling concentration systems of heater and II effect evaporator composition, II effect evaporator top vacuum holding -0.08Mpa, temperature
Degree maintains 80 DEG C, and temperature is 90 DEG C after II effect Roots's methanol compressor；During dual evaporation, methanol constantly produces, concentration
About 90~95%；After about 80 DEG C of saturated ammonium chloride solution is thickened into thickener in II effect evaporator, feed liquid is put into
Centrifuge isolates white ammonium chloride product, purity of ammonia chloride 99.1%.Ammonia nitrogen recovery rate more than 97.5%.
Embodiment 3
Methanol and ammonium chloride extraction equipment in a kind of glycine production, conveying pipeline are connected through feed pump 1 with preheater 2, in advance
The hot top of device 2 is connected with I effect heaters A 3, and I effect heaters A 3 is connected with I effect evaporators 5, and the I effect bottoms of evaporator 5 are imitated with I
Heater B 4 is connected, and the bottoms of I effect heaters B 4 imitate heater A 3 with I through circulating pump 9 and are connected formation circulation；
I effect heaters A 3, the bottoms of I effect heaters B 4 are connected through conveying pipeline with methanol discharge tank 8；
The I effects bottom of evaporator 5 is connected through conveying pipeline with turning batch can 11, is turned batch can 11 and is imitated heater 14 through transfering material pump 13 and II
Connection, II are imitated heater 14 and are connected with II effect evaporators 15；
The II effects bottom of evaporator 15 is connected with thickener 20, and thickener 20 connects with mother liquor pond 19 again after being connected with centrifuge 21
Connect.
The described top of I effects evaporator 5 is connected with I effect Roots's methanol compressor 6, and I imitates Roots's methanol compressor 6 through oxygen
In-line analyzer 7 is connected with I effect heaters A 3, I effect heaters B 4 respectively, and methanol discharge tank 8 is imitated through methanol discharging pump 22 and I
Roots's methanol compressor 6 connects, and forms circulating system.
The described II effects bottom of evaporator 15 is connected through conveying pipeline with forced circulation pump 17, and forced circulation pump 17 and II effects add
Hot device 14 connects, and II is imitated heater 14 and is connected with II effect evaporators 15；Described mother liquor pond 19 is through mother liquor reflux pump (18) and by force
Circulating pump 17 processed connects.
The described top of II effects evaporator 15 is imitated Roots's methanol compressor 16 through II and connected, II effect Roots's methanol compressor 16
Divide two-way, be connected, be connected all the way with condenser 12, condenser (12) with I effect heaters A 3, I effect heaters B 4 respectively all the way
It is connected with dilute methanol tank 10, methanol discharge tank 8 is imitated Roots's methanol compressor (16) with II through methanol discharging pump 22 and is connected, and formation follows
Member ring systems.
Claims (4)
1. methanol and ammonium chloride extraction equipment in a kind of glycine production, it is characterised in that conveying pipeline is through feed pump（1）With preheating
Device（2）Connection, preheater（2）Top and I effect heaters A（3）Connection, I effect heaters A（3）Evaporator is imitated with I（5）Connection, I
Imitate evaporator（5）Bottom and I effect heaters B（4）Connection, I effect heaters B（4）Bottom is through circulating pump（9）With I effect heaters A
（3）Connection forms circulation；
I effect heaters A（3）, I effects heater B（4）Bottom is through conveying pipeline and methanol discharge tank（8）Connection；
I imitates evaporator（5）Bottom is through conveying pipeline and turns batch can（11）Connection, turns batch can（11）Through transfering material pump（13）Add with II effects
Hot device（14）Connection, II effect heaters（14）Evaporator is imitated with II（15）Connection；
II imitates evaporator（15）Bottom and thickener（20）Connection, thickener（20）With centrifuge（21）After connection again with mother liquor pond
（19）Connection.
2. methanol and ammonium chloride extraction equipment in the glycine production described in claim 1, it is characterised in that described I effects are steamed
Send out device（5）Top and I effect Roots's methanol compressors（6）Connection, I effect Roots's methanol compressors（6）Through oxygen in-line analyzer（7）
Respectively heater A is imitated with I（3）, I effects heater B（4）Connection, methanol discharge tank（8）Through methanol discharging pump（22）Roots is imitated with I
Methanol compressor（6）Connection, form circulating system.
3. methanol and ammonium chloride extraction equipment in the glycine production described in claim 1, it is characterised in that described II effects are steamed
Send out device（15）Bottom is through conveying pipeline and forced circulation pump（17）Connection, forced circulation pump（17）Heater is imitated with II（14）Connection,
II imitates heater（14）Evaporator is imitated with II（15）Connection；Described mother liquor pond（19）Through mother liquor reflux pump（18）With forced circulation
Pump（17）Connection.
4. methanol and ammonium chloride extraction equipment in the glycine production described in claim 1, it is characterised in that described II effects are steamed
Send out device（15）Roots's methanol compressor is imitated through II in top（16）Connection, II effect Roots's methanol compressors（16）Divide two-way, divide all the way
Heater A is not imitated with I（3）, I effects heater B（4）Connection, all the way with condenser（12）Connection, condenser（12）With dilute methanol tank
（10）Connection, methanol discharge tank（8）Through methanol discharging pump（22）Roots's methanol compressor is imitated with II（16）Connection, form loop body
System.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720307079.1U CN206654738U (en) | 2017-03-27 | 2017-03-27 | Methanol and ammonium chloride extraction equipment in a kind of glycine production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720307079.1U CN206654738U (en) | 2017-03-27 | 2017-03-27 | Methanol and ammonium chloride extraction equipment in a kind of glycine production |
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| Publication Number | Publication Date |
|---|---|
| CN206654738U true CN206654738U (en) | 2017-11-21 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106830010A (en) * | 2017-03-27 | 2017-06-13 | 湖北兴发化工集团股份有限公司 | Methyl alcohol and ammonium chloride extraction equipment and extraction process in a kind of glycine production |
-
2017
- 2017-03-27 CN CN201720307079.1U patent/CN206654738U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106830010A (en) * | 2017-03-27 | 2017-06-13 | 湖北兴发化工集团股份有限公司 | Methyl alcohol and ammonium chloride extraction equipment and extraction process in a kind of glycine production |
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