CN109651067A - A kind of preparation process of 1,1,2- trichloroethanes - Google Patents
A kind of preparation process of 1,1,2- trichloroethanes Download PDFInfo
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- CN109651067A CN109651067A CN201811654100.0A CN201811654100A CN109651067A CN 109651067 A CN109651067 A CN 109651067A CN 201811654100 A CN201811654100 A CN 201811654100A CN 109651067 A CN109651067 A CN 109651067A
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- trichloroethanes
- liquid
- tower
- boiling tower
- alkali cleaning
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- UBOXGVDOUJQMTN-UHFFFAOYSA-N 1,1,2-trichloroethane Chemical class ClCC(Cl)Cl UBOXGVDOUJQMTN-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 238000002360 preparation method Methods 0.000 title claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 59
- 238000009835 boiling Methods 0.000 claims abstract description 41
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000003513 alkali Substances 0.000 claims abstract description 27
- 238000004140 cleaning Methods 0.000 claims abstract description 24
- 239000000460 chlorine Substances 0.000 claims abstract description 18
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 17
- 239000012043 crude product Substances 0.000 claims abstract description 15
- 239000000463 material Substances 0.000 claims abstract description 14
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 11
- UOCLXMDMGBRAIB-UHFFFAOYSA-N 1,1,1-trichloroethane Chemical class CC(Cl)(Cl)Cl UOCLXMDMGBRAIB-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000000126 substance Substances 0.000 claims abstract description 9
- 238000003860 storage Methods 0.000 claims abstract description 8
- 239000000047 product Substances 0.000 claims abstract description 6
- 239000002808 molecular sieve Substances 0.000 claims abstract description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 41
- 239000002351 wastewater Substances 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 7
- 239000000243 solution Substances 0.000 claims description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 6
- 238000002309 gasification Methods 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 3
- 238000007259 addition reaction Methods 0.000 claims description 3
- 150000001336 alkenes Chemical class 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 claims description 3
- 150000001804 chlorine Chemical class 0.000 claims description 3
- 230000001276 controlling effect Effects 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 239000010413 mother solution Substances 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 238000005070 sampling Methods 0.000 claims description 3
- 159000000000 sodium salts Chemical class 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 2
- 230000001376 precipitating effect Effects 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 6
- 238000002347 injection Methods 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- OEPOKWHJYJXUGD-UHFFFAOYSA-N 2-(3-phenylmethoxyphenyl)-1,3-thiazole-4-carbaldehyde Chemical compound O=CC1=CSC(C=2C=C(OCC=3C=CC=CC=3)C=CC=2)=N1 OEPOKWHJYJXUGD-UHFFFAOYSA-N 0.000 description 1
- 125000001340 2-chloroethyl group Chemical class [H]C([H])(Cl)C([H])([H])* 0.000 description 1
- GZETWZZNDACBTQ-UHFFFAOYSA-N [Cl].C=C Chemical group [Cl].C=C GZETWZZNDACBTQ-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- -1 chloroethene Alkene Chemical class 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/013—Preparation of halogenated hydrocarbons by addition of halogens
- C07C17/04—Preparation of halogenated hydrocarbons by addition of halogens to unsaturated halogenated hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of preparation processes of 1,1,2- trichloroethanes, the preparation process include the following steps: (1) by vinyl chloride with chlorine be sent into chlorination reactor, the 1,1 of generation, 2 ,-trichloroethanes a part is by chlorination reactor top overflow port overflow to chlorated liquid storage tank；(2) chlorated liquid in chlorated liquid storage tank is squeezed into and carries out alkali cleaning in alkali cleaning kettle, be then allowed to stand layering, lower layer is that colourless transparent liquid places 1,1,2- trichloroethanes crude product slot squeezes into 1,1,2- trichloroethanes crude product large trough for trichloroethanes rectifying using alkali cleaning trichloroethanes intermediate pump；(3) by 1,1,2- trichloroethanes crude product by low boiling tower, liquid enters trichloroethanes low-boiling-point substance collecting tank, and materials at bottom of tower is pumped into high boiling tower by high boiling tower feed pump and is refined；(4) into the material of high boiling tower through high boiling tower rectifying again, liquid enters molecular sieve tank and enters 1,1,2- trichloroethanes finished product large trough using liquid level difference.The present invention has the advantages that the present invention can save resource and reduce production cost.
Description
Technical field
The invention belongs to chemical fields, are related to a kind of technique for producing 1,1,2- trichloroethanes, specifically a kind of with chlorine
Ethylene is the technique that raw material prepares 1,1,2- trichloroethanes.
Background technique
1,1,2- trichloroethanes is a kind of important industrial chemicals, can be used for preparing the chemical products such as vinylidene chloride.1,
1,2- trichloroethanes is usually using vinyl chloride and chlorine as the chlorizate of raw material.Reaction equation are as follows:。
Many documents and patent disclose 1,1,2- trichloroethanes of preparation, as patent CN 100335450C discloses one kind
1,1,2- trichloroethanes is prepared, includes the following steps: with 1,1,2- trichloroethanes to be sent into the first mixing jetting for circulatory mediator
Device, vinyl chloride are pumped into the mixed zone of the first mixed injection device by the vinyl chloride entrance of the first mixed injection device,
The vinyl chloride for being then dissolved in 1,1,2- trichloroethanes is sent into the second mixed injection device, and chlorine is filled by the second mixing jetting
The chlorine inlet set is pumped into the mixed zone of the second mixed injection device, in the mixed zone of the second mixed injection device, chloroethene
Alkene and chlorine mixing pre-reaction, subsequently into the main pipeline reactor equipped with static mixing element, the reaction was continued, generates 1,1,2-
Trichloroethanes, the product after reaction, by gas-liquid separator separates, into subsequent workshop section, conversion rate of vinyl chloride can reach 98% with
On, selection rate can reach 96% or more, use convenient for industrialization promotion；But the production method has some disadvantages: producing
It is needed in journey using mixed injection device and the main pipeline reactor equipped with static mixing element, these apparatus structures are relatively multiple
Miscellaneous, occupied space is big, and then will increase production cost；Meanwhile the by-product generated in production process, benefit cannot be recycled
With waste of resource significantly further increases production cost.
Therefore, a kind of preparation process right and wrong of 1,1,2- trichloroethanes that can be saved resource and reduce production cost are researched and developed
Often it is necessary to.
Summary of the invention
Resource can be saved the technical problem to be solved in the present invention is to provide one kind and reduces the 1,1,2- tri- of production cost
The preparation process of chloroethanes.
In order to solve the above technical problems, the technical solution of the present invention is as follows: a kind of preparation process of 1,1,2- trichloroethanes,
Innovative point is: the preparation process includes the following steps:
Step 1: chlorine addition: the material in vinyl chloride slot being squeezed into vinyl chloride head tank by canned motor pump and is controlled through regulating valve A
Enter vinyl chloride evaporator using liquid level difference, reaches vinyl chloride flowmeter through vinyl chloride surge tank again after gasification；Liquid chlorine passes through chlorine
Gas cylinder enters chlorine salt water vaporization pond through regulating valve B control, reaches cl gas flow meter through Chlorine Buffer Vessel after gasification；Then will
Vinyl chloride enters chlorination reactor with the flow that chlorine is 1:1.05~1.1 in molar ratio, under the action of iron hoop is catalyst
Addition reaction is carried out, control reaction temperature is 40 DEG C~45 DEG C, and reaction heat pumps forced circulation by circulated chlorination, passes through condenser
Recirculated water is taken away, and the 1 of generation, 1,2 ,-trichloroethanes a part participates in Recycling Mother Solution, and a part is overflow by chlorination reactor top
Head piece overflow is to chlorated liquid storage tank；
Step 2: alkali cleaning layering: opening alkali cleaning kettle vacuum valve, starts vacuum NaOH solution circulating pump, under vacuum conditions, by chlorated liquid
Chlorated liquid in storage tank is squeezed into alkali cleaning kettle by chlorated liquid dnockout pumps, is reached and is stopped chlorated liquid dnockout pump startup after regulation liquid level and stir
Motor is mixed, stirs 15~25min under vacuum conditions, during this, portion is escaped from chlorated liquid, passes through vacuum lye
It is absorbed, is switched as NaOH<1%, NaClO>=10% in vacuum lye, sodium hypochlorite is pumped by vacuum NaOH solution circulating pump
In slot, closes vacuum valve opening exhaust valve and the liquid alkaline in alkali measuring tank is added dropwise in alkali cleaning kettle, it is cold using alkali cleaning kettle collet
But circulation water management alkali cleaning kettle temperature degree is terminated when sampling analysis top high-salt wastewater pH value is 7~8 and is added dropwise between 20~30 DEG C
Liquid alkaline, is then allowed to stand layering, stands and is shown on trial blowing after 20~40min from bottom subordinate material, lower layer is that colourless transparent liquid is placed
1,1,2- trichloroethanes crude product slot squeezes into 1,1,2- trichloroethanes crude product large trough for three chloroethenes using alkali cleaning trichloroethanes intermediate pump
Alkane rectification is used, and upper layer is put into alkali-wash waste water intermediate pool for yellowish high-salt wastewater and squeezes into three-level precipitating through high-salt wastewater rear pump again
Pond, after triple effect evaporation, concentration, reuse between the secondary steam waterwheel of generation, sodium salt sells processing outside；
Step 3: a rectifying: by 1,1,2- trichloroethanes crude product large trough by dnockout pumps, squeezing into 1,1,2- trichloroethanes of crude product
Head tank enters low boiling tower using liquid level difference, is heated to 105~115 DEG C through low boiling tower reboiler, low-boiling-point substance therein is converted
It is 95~105 DEG C through low boiling tower overhead condenser control tower top temperature, gas is through low boiling tower complete condenser and low boiling tower tail for gas
After gas condenser is cooling, liquid enters trichloroethanes low-boiling-point substance collecting tank, and materials at bottom of tower is pumped into high boiling by high boiling tower feed pump
Tower is refined；
Step 4: secondary rectifying: the material into high boiling tower is heated to 115~125 DEG C through high boiling tower reboiler, by 1,1,2- tri-
Chloroethanes is converted into gas, and controlling tower top temperature by high boiling tower overhead condenser is 112~116 DEG C, and gas is complete through high boiling tower
After condenser and high boiling tower tail gas condenser are cooling, liquid enters molecular sieve tank and enters 1,1,2- trichloroethanes finished product using liquid level difference
Large trough.
Further, in the step 1 internal pressure of vinyl chloride slot and vinyl chloride head tank control 0.2~
0.3MPa, temperature are controlled at 15~25 DEG C.
Further, the collet hot water temperature of vinyl chloride evaporator controls at 45~55 DEG C in the step 1.
Further, liquid alkaline is added dropwise in the step 2, it is 15%~18% liquid alkaline that liquid alkaline, which selects mass percentage concentration,.
The present invention has the advantages that the preparation process of 1,1,2- trichloroethanes of the invention, using vinyl chloride and chlorine as raw material,
It is reacted by conventional chemical production equipment, mild condition, the 1,1,2 of chlorination reaction generation ,-trichloroethanes a part is participated in
Recycling Mother Solution can make generate 1,1,2, and-trichloroethanes can be recycled, and the high-salt wastewater in lye layering is then
After triple effect evaporation, concentration, reuse between the secondary steam waterwheel of generation, the by-product which can be such that each step generates
Object is recycled, and resource can be greatlyd save, furthermore, it is possible to further decrease production cost.
Detailed description of the invention
The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.
Fig. 1 is the flow chart of the preparation process of 1,1,2- trichloroethanes of the present invention.
Specific embodiment
The following examples can make professional and technical personnel that the present invention be more fully understood, but therefore not send out this
It is bright to be limited among the embodiment described range.
Embodiment
The present embodiment 1,1, the preparation process of 2- trichloroethanes, the preparation process include the following steps:
Step 1: chlorine addition: by internal pressure control in 0.25MPa, material of the temperature control in 20 DEG C of vinyl chloride slot is logical
It crosses canned motor pump and squeezes into internal pressure control in 0.25MPa, temperature control controls benefit through regulating valve A in 20 DEG C of vinyl chloride head tank
Enter vinyl chloride evaporator with liquid level difference, the collet hot water temperature of vinyl chloride evaporator controls at 50 DEG C, again through chloroethene after gasification
Alkene surge tank reaches vinyl chloride flowmeter；Liquid chlorine enters chlorine salt water vaporization pond, gasification through regulating valve B control by chlorine cylinder
Cl gas flow meter is reached by Chlorine Buffer Vessel；It then is in molar ratio that the flow of 1:1.075 enters chlorine with chlorine by vinyl chloride
Change reactor, carry out addition reaction under the action of iron hoop is catalyst, control reaction temperature is 40 DEG C~45 DEG C, reaction heat by
Circulated chlorination pumps forced circulation, is taken away by the recirculated water of condenser, the 1 of generation, 1,2, and-trichloroethanes a part participates in mother liquor
Circulation, a part is by chlorination reactor top overflow port overflow to chlorated liquid storage tank；
Step 2: alkali cleaning layering: opening alkali cleaning kettle vacuum valve, starts vacuum NaOH solution circulating pump, under vacuum conditions, by chlorated liquid
Chlorated liquid in storage tank is squeezed into alkali cleaning kettle by chlorated liquid dnockout pumps, is reached and is stopped chlorated liquid dnockout pump startup after regulation liquid level and stir
Motor is mixed, stirs 20min under vacuum conditions, during this, portion is escaped from chlorated liquid, is carried out by vacuum lye
It absorbs, switches as NaOH<1%, NaClO>=10% in vacuum lye, sodium hypochlorite slot is pumped by vacuum NaOH solution circulating pump
In, it closes vacuum valve opening exhaust valve and the liquid alkaline that mass percentage concentration is 16% in alkali measuring tank, benefit is added dropwise in alkali cleaning kettle
With alkali cleaning kettle collet cooling cycle water management alkali cleaning kettle temperature degree between 20~30 DEG C, sampling analysis top high-salt wastewater pH value is
It is terminated when 7~8 and liquid alkaline is added dropwise, be then allowed to stand layering, stood and shown on trial blowing after 30min from bottom subordinate material, lower layer is colourless
Prescribed liquid places 1,1,2- trichloroethanes crude product slot, and using alkali cleaning trichloroethanes intermediate pump to squeeze into 1,1,2- trichloroethanes crude product big
Slot is put into alkali-wash waste water intermediate pool for yellowish high-salt wastewater and beats again through high-salt wastewater rear pump for trichloroethanes rectifying, upper layer
Enter three-level sedimentation basin, after triple effect evaporation, concentration, reuse between the secondary steam waterwheel of generation, sodium salt sells processing outside；
Step 3: a rectifying: by 1,1,2- trichloroethanes crude product large trough by dnockout pumps, squeezing into 1,1,2- trichloroethanes of crude product
Head tank enters low boiling tower using liquid level difference, is heated to 110 DEG C through low boiling tower reboiler, converts gas for low-boiling-point substance therein
Body is 100 DEG C through low boiling tower overhead condenser control tower top temperature, and gas is through low boiling tower complete condenser and low boiling tower tail gas condenser
After cooling, liquid enters trichloroethanes low-boiling-point substance collecting tank, and materials at bottom of tower is pumped into high boiling tower by high boiling tower feed pump and carries out essence
System；
Step 4: secondary rectifying: the material into high boiling tower is heated to 120 DEG C through high boiling tower reboiler, by 1,1,2- trichloroethanes
It is converted into gas, controlling tower top temperature by high boiling tower overhead condenser is 114 DEG C, and gas is through high boiling tower complete condenser and high boiling tower
After tail gas condenser is cooling, liquid enters molecular sieve tank and enters 1,1,2- trichloroethanes finished product large trough using liquid level difference.
The present embodiment 1,1, in the preparation process of 2- trichloroethanes, conversion rate of vinyl chloride can reach 98.5%, and selection rate is reachable
To 96.8%.
Basic principles and main features and advantages of the present invention of the invention have been shown and described above.The skill of the industry
Art personnel it should be appreciated that the present invention is not limited to the above embodiments, the above embodiments and description only describe
The principle of the present invention, without departing from the spirit and scope of the present invention, various changes and improvements may be made to the invention, these
Changes and improvements all fall within the protetion scope of the claimed invention.The claimed scope of the invention by appended claims and
Its equivalent thereof.
Claims (4)
1. one kind 1,1, the preparation process of 2- trichloroethanes, it is characterised in that: the preparation process includes the following steps:
Step 1: chlorine addition: the material in vinyl chloride slot being squeezed into vinyl chloride head tank by canned motor pump and is controlled through regulating valve A
Enter vinyl chloride evaporator using liquid level difference, reaches vinyl chloride flowmeter through vinyl chloride surge tank again after gasification；Liquid chlorine passes through chlorine
Gas cylinder enters chlorine salt water vaporization pond through regulating valve B control, reaches cl gas flow meter through Chlorine Buffer Vessel after gasification；Then will
Vinyl chloride enters chlorination reactor with the flow that chlorine is 1:1.05~1.1 in molar ratio, under the action of iron hoop is catalyst
Addition reaction is carried out, control reaction temperature is 40 DEG C~45 DEG C, and reaction heat pumps forced circulation by circulated chlorination, passes through condenser
Recirculated water is taken away, and the 1 of generation, 1,2 ,-trichloroethanes a part participates in Recycling Mother Solution, and a part is overflow by chlorination reactor top
Head piece overflow is to chlorated liquid storage tank；
Step 2: alkali cleaning layering: opening alkali cleaning kettle vacuum valve, starts vacuum NaOH solution circulating pump, under vacuum conditions, by chlorated liquid
Chlorated liquid in storage tank is squeezed into alkali cleaning kettle by chlorated liquid dnockout pumps, is reached and is stopped chlorated liquid dnockout pump startup after regulation liquid level and stir
Motor is mixed, stirs 15~25min under vacuum conditions, during this, portion is escaped from chlorated liquid, passes through vacuum lye
It is absorbed, is switched as NaOH<1%, NaClO>=10% in vacuum lye, sodium hypochlorite is pumped by vacuum NaOH solution circulating pump
In slot, closes vacuum valve opening exhaust valve and the liquid alkaline in alkali measuring tank is added dropwise in alkali cleaning kettle, it is cold using alkali cleaning kettle collet
But circulation water management alkali cleaning kettle temperature degree is terminated when sampling analysis top high-salt wastewater pH value is 7~8 and is added dropwise between 20~30 DEG C
Liquid alkaline, is then allowed to stand layering, stands and is shown on trial blowing after 20~40min from bottom subordinate material, lower layer is that colourless transparent liquid is placed
1,1,2- trichloroethanes crude product slot squeezes into 1,1,2- trichloroethanes crude product large trough for three chloroethenes using alkali cleaning trichloroethanes intermediate pump
Alkane rectification is used, and upper layer is put into alkali-wash waste water intermediate pool for yellowish high-salt wastewater and squeezes into three-level precipitating through high-salt wastewater rear pump again
Pond, after triple effect evaporation, concentration, reuse between the secondary steam waterwheel of generation, sodium salt sells processing outside；
Step 3: a rectifying: by 1,1,2- trichloroethanes crude product large trough by dnockout pumps, squeezing into 1,1,2- trichloroethanes of crude product
Head tank enters low boiling tower using liquid level difference, is heated to 105~115 DEG C through low boiling tower reboiler, low-boiling-point substance therein is converted
It is 95~105 DEG C through low boiling tower overhead condenser control tower top temperature, gas is through low boiling tower complete condenser and low boiling tower tail for gas
After gas condenser is cooling, liquid enters trichloroethanes low-boiling-point substance collecting tank, and materials at bottom of tower is pumped into high boiling by high boiling tower feed pump
Tower is refined；
Step 4: secondary rectifying: the material into high boiling tower is heated to 115~125 DEG C through high boiling tower reboiler, by 1,1,2- tri-
Chloroethanes is converted into gas, and controlling tower top temperature by high boiling tower overhead condenser is 112~116 DEG C, and gas is complete through high boiling tower
After condenser and high boiling tower tail gas condenser are cooling, liquid enters molecular sieve tank and enters 1,1,2- trichloroethanes finished product using liquid level difference
Large trough.
2. according to claim 11, the preparation process of 1,2- trichloroethanes, it is characterised in that: chloroethene in the step 1
The internal pressure of alkene slot and vinyl chloride head tank is controlled in 0.2~0.3MPa, and temperature is controlled at 15~25 DEG C.
3. according to claim 11, the preparation process of 1,2- trichloroethanes, it is characterised in that: chloroethene in the step 1
The collet hot water temperature of alkene evaporator controls at 45~55 DEG C.
4. according to claim 11, the preparation process of 1,2- trichloroethanes, it is characterised in that: be added dropwise in the step 2
Liquid alkaline, it is 15%~18% liquid alkaline that liquid alkaline, which selects mass percentage concentration,.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110511110A (en) * | 2019-08-09 | 2019-11-29 | 浙江衢州巨塑化工有限公司 | A kind of 1,1,2- trichloroethanes reactor and its method |
| CN112479804A (en) * | 2019-09-12 | 2021-03-12 | 南京延长反应技术研究院有限公司 | System and process for strengthening chloroethane preparation based on micro-interface |
| CN113121303A (en) * | 2021-04-26 | 2021-07-16 | 河北美邦工程科技股份有限公司 | Chloroethylene production process and special device thereof |
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