CN106621715A - Device for recovering chlorine hydride in PVC production process - Google Patents
Device for recovering chlorine hydride in PVC production process Download PDFInfo
- Publication number
- CN106621715A CN106621715A CN201710010325.1A CN201710010325A CN106621715A CN 106621715 A CN106621715 A CN 106621715A CN 201710010325 A CN201710010325 A CN 201710010325A CN 106621715 A CN106621715 A CN 106621715A
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- Prior art keywords
- acid
- hydrochloric acid
- pvc production
- tower
- production processes
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- 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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
-
- 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
- B01D53/14—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 by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/202—Single element halogens
- B01D2257/2025—Chlorine
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a device for recovering chlorine hydride in the PVC production process and a chlorine hydride combined-absorption tower. The chlorine hydride combined-absorption tower comprises a gas inlet, a discharging port, an isothermal absorption zone, a concentrated acid absorption zone, a diluted acid absorption zone, a clear water absorption zone and a tower top exhausting port. The discharging port is connected with a concentrated acid tank, and the concentrated acid tank is connected with a hydrochloric acid desorption device. The hydrochloric acid desorption device comprises an exhausting pipeline provided with a drying device and a diluted acid discharging pipeline. The diluted acid discharging pipeline is connected with a diluted hydrochloric acid desorption device. The device is small in occupied area, and the investment cost can be saved.
Description
Technical field
The present invention relates to vinyl chloride production technology and device, are hydrogen chloride in a kind of PVC production processes specifically
Retracting device.
Background technology
In prior art, in the technical process by acetylene and hcl reaction synthesis vinyl chloride thereof, in order to improve acetylene
Conversion ratio, not only economic but also feasible method was to allow unstripped gas chlorination excess hydrogen.In actual production process, acetylene and hydrogen chloride are logical
Often it is controlled to n (C2H2): n (HCl)=1: (1.05-1.10), existing excess hydrogen chloride in VCM production handling process
Process is that vinyl chloride thick first out, into mercury eliminator charcoal absorption chlorine high mercury compound is mainly contained by converter
After mercuryvapour, enter back into synthesis gas graphite cooler and temperature be cooled to into 15 DEG C or so falling film absorption systems of being allowed for access, with by
The watery hydrochloric acid that sieve-plate tower is flowed into absorbs the hydroperoxide in synthesis gas, and the by-product hydrochloric acid of 25-28% is obtained.Synthesis gas after relieving haperacidity
Sieve-plate tower is successively entered, water scrubber and caustic wash tower are purified, and absorb the miscellaneous gas such as remaining hydrogen chloride and carbon dioxide, obtain what is refined
Vinyl chloride will keep certain liquid circulation amount for polymerization, washing, caustic wash tower, and to meet the needs of purification, fresh water is from water
Wash tower to be continuously added to, waste liquid is also continuously discharged, small part is flowed into and enter after sieve-plate tower falling film absorption system relieving haperacidity, alkali lye then timing
Change, certain density sodium hydroxide solution must be changed as absorbing liquid after wherein concentration of sodium carbonate is exceeded.Using above-mentioned
Equipment, hydrogen chloride cannot circulation and stress as synthesis vinyl chloride thereof unstripped gas, produced accessory substance is difficult to direct marketing
The mercurous hydrochloric acid of low concentration；And technological process is long, the device for using is more, and sieve-plate tower operating flexibility is little, and pressure drop is high, process operation
Control is difficult.
The content of the invention
It is an object of the invention to provide chlorination hydrogen recovery unit in a kind of PVC production processes, to realize PVC production processes
The circulation and stress of middle hydrogen chloride.
To achieve these goals, the technical solution used in the present invention is：Chlorination hydrogen retrieval dress in a kind of PVC production processes
Put, including：Hydrogen chloride combined absorbing tower, described hydrogen chloride combined absorbing tower from bottom to top include successively air inlet, discharging opening,
Isothermal uptake zone, concentrated acid uptake zone, diluted acid uptake zone, clear water uptake zone and tower top exhaust outlet；The discharging opening is connected with concentrated acid
Tank, the concentrated acid tank connects hydrochloric acid desorption device；The hydrochloric acid desorption device includes being provided with the discharge duct of drying device and dilute
Sour discharge line；The diluted acid discharge line connects watery hydrochloric acid desorption device.
Preferably, described isothermal uptake zone is provided with graphite falling film absorber.
Preferably, described concentrated acid uptake zone is packing area.
Preferably, described hydrochloric acid desorption device also includes hydrochloric acid head tank and sulfuric acid high position tank, the sulfuric acid high position tank
Connection extractant middle part.
Preferably, the material of described extractor is high temperature resistant and corrosion-resistant material, preferably high silicon ceramic material.
Preferably, the extractor top tower body diameter and lower groove body diameter ratio are 1: 1.8-1: 2.5.
The beneficial effects of the present invention is：Used in the present invention is hydrogen chloride combined absorbing tower, chlorination hydrogen recovery process
Middle flow process is simplified, and device used is few, and floor space is little, and can reduce investment outlay expense；The special of combined absorbing tower sets
Meter, employs proprietary falling-film absorber and filler Deethanizer design, and process control is convenient；A large amount of hydrogen chloride flows are allowed in start-up
Enter device, and process overtemperature will not be caused, it is to avoid a large amount of hydrogen chloride of start-up enter system in traditional handicraft, easily cause
Process overtemperature is so as to damaging the problem of device.
Description of the drawings
The Figure of description for constituting the part of the application is used for providing a further understanding of the present invention, and the present invention's shows
Meaning property embodiment and its illustrated for explaining the present invention, does not constitute inappropriate limitation of the present invention.In the accompanying drawings：
Fig. 1 reclaims schematic diagram entirely for excess hydrogen chloride in VCM production of the present invention.
Specific embodiment
It should be noted that in the case where not conflicting, the feature in embodiment and embodiment in the application can phase
Mutually combination.Below with reference to the accompanying drawings and in conjunction with the embodiments describing the present invention in detail.
It is noted that described further below is all exemplary, it is intended to provide further instruction to the application.Unless another
Indicate, all technologies used herein and scientific terminology are with usual with the application person of an ordinary skill in the technical field
The identical meanings of understanding.
The technical scheme in the embodiment of the present invention will be clearly and completely described below, it is clear that described enforcement
Example is only a part of embodiment of the present invention, rather than the embodiment of whole.Based on the embodiment in the present invention, this area is common
All other embodiment that technical staff is obtained under the premise of creative work is not made, belongs to the model of present invention protection
Enclose.
Chlorination hydrogen recovery unit in a kind of PVC production processes as described in Figure 1, including：Hydrogen chloride combined absorbing tower, it is described
Hydrogen chloride combined absorbing tower from bottom to top successively include air inlet, discharging opening, isothermal uptake zone, concentrated acid uptake zone, diluted acid inhale
Receive area, clear water uptake zone and tower top exhaust outlet；The discharging opening is connected with concentrated acid tank, the concentrated acid tank connection hydrochloric acid desorption dress
Put；The hydrochloric acid desorption device includes being provided with the discharge duct and diluted acid discharge line of drying device；The diluted acid discharge line
Connection watery hydrochloric acid desorption device.
40 DEG C of pressure enters for the vinyl chloride mixed gas of the 5400m3/h containing hydrogen chlorides of 10kPa from the bottom of combined column 1
Gas port is entered, and first passes around an isothermal uptake zone 1a, and the temperature of the vinyl chloride mixed gas of containing hydrogen chloride is gradually reduced, chlorination
Hydrogen is partly absorbed.Absorber used is proprietary graphite falling film absorber, hydrogen chloride gas and pipe (or short-bore)
The equally distributed liquid film in surface is absorbed after being fully contacted, and liberated heat is removed by the cooling water of shell side.
The concentrated acid uptake zone 1b on upper strata, i.e., one layer packing area are entered through the mixed gas of isothermal uptake zone 1a.Through etc.
The mixed gas of warm uptake zone 1a are then entered from the lower section of one layer of packing area, by the free space in the filler gap of packing area,
The liquid for not having a part of filled surface of absorbed hydrogen chloride gas in isothermal uptake zone is absorbed, unabsorbed gas
Body enters the top of concentrated acid uptake zone.
Continue to rise from concentrated acid uptake zone mixed gas out, into the diluted acid uptake zone 1c on upper strata, i.e., two layers filler
Area, after being absorbed, continues to rise from diluted acid uptake zone 1c mixed gas out, into the clear water uptake zone 1d on upper strata, i.e.,
Sieve plate area.Absorption process in this area is also the process of adiabatic absorption, and unabsorbed remaining hydrogen chloride gas are inhaled by water
Receive.
Through above-mentioned this series of process, the purity from vinyl chloride in the gas out of combined absorbing tower top is very high,
Most hydrogen chloride gas are absorbed, hydrogen chloride content 0.05% in the vinyl chloride gaseous mixture of discharge, described mixed gas
At 25 DEG C, pressure is 6kPa, and 4700m3/h is discharged from tower top, send combination caustic wash tower further to refine.Clear water connects from top layer column plate
Continuous to add, concentration is that 30% concentrated hydrochloric acid is continuously discharged by absorption tower bottom discharge mouth.This acid can be used as desorption raw material desorption system
Hydrogen chloride gas return to synthesis post for synthesis vinyl chloride thereof.
The concentrated hydrochloric acid discharged from the discharging opening of combined column 1 is introduced in concentrated acid tank 4, is carried out subsequently into hydrochloric acid desorption system 2
Desorption.After hydrochloric acid desorption system 2, the concentration of hydrochloric acid drops to 19% or so, and the hydrogen chloride gas of desorption are de- from the hydrochloric acid
Discharge in desorption system 2, synthesis procedure synthesis vinyl chloride thereof is entered after being fully dried.Meanwhile, remaining 19% diluted acid is entered
Store in diluted acid tank 5.Diluted acid tank 5 is deeply de- with the concentrated acid uptake zone 1b and watery hydrochloric acid of combined absorbing tower 1 respectively by pipeline
Desorption system 3 is connected.Into watery hydrochloric acid depth desorption system 3 19% hydrochloric acid after the system, the concentration of hydrochloric acid drops to little
In 1%, the hydrogen chloride gas of desorption are discharged from the desorption system outlet, and synthesis procedure synthesis vinyl chloride thereof is entered after being fully dried.
The concentration of hydrochloric acid drops to less than 1% in solution after desorption, when the water of the top clear water uptake zone absorbent of combined absorbing tower 1
Amount derives from this,
The watery hydrochloric acid depth desorption method that the present embodiment is adopted is for concentrated sulfuric acid desorption method：
It is comprised the following steps that：
21% watery hydrochloric acid, 98% concentrated sulfuric acid respectively enter hydrochloric acid tank and sulphuric acid tank, then respectively by hydrochloric acid pump and sulphur
Sour pump squeezes into hydrochloric acid head tank and sulfuric acid high position tank, first that hydrochloric acid is high in the case of the overflow liquid back pipe of two head tanks is normal
The hydrochloric acid of position groove enters the top of extractor Jing after flowmeter adjusts metering, and wherein the concentrated sulfuric acid and the volume ratio of watery hydrochloric acid are 2: 1
The sulfuric acid of sulfuric acid high position tank is entered again the middle part of extractor Jing after Flow-rate adjustment metering, two kinds of acid are continuous in extractor cell body
Overflow, mixing, the hydrogen chloride for extracting leaves liquid level from cell body, constantly rises in tower body above, and Jing is top-down
The concentrated sulfuric acid draws extractor after being dried, into hydrogen chloride gas holder.Described extractor is the diameter and lower groove body of top tower body
Diameter ratio be 1: 2, be by high silicon ceramic material extractor.Two extractors are only out one for one with one, extractor
Diameter foot is amplified and is conducive to gas diffusion, improves desorption effect.
From the mixed acid that extractor and extractor cell body bottom flow out, nitration mixture groove is entered Jing after graphite cooler cooling,
Dechlorinator is squeezed into by nitration mixture pump, the gas after dechlorination is emptied Jing after tail gas absorber washing.
The concentration of sulfuric acid is 70% sulfuric acid in mixed acid from dechlorinator out, in being stored in sulfuric acid tank, so
Squeezed in sulfuric acid concentrate device by sulfuric acid pump again afterwards, the sulfuric acid being added thereto using open firing in sulfuric acid concentrate device so as to temperature
360 DEG C are risen to, the moisture in sulfuric acid is evaporated, at high temperature concentrated vitriol, until the sulfuric acid taken out from sulfuric acid concentrate device middle part
Concentration up to 97%.In heating up process, sulfuric acid vapor is first released from tower top and enters stripper, from sulfuric acid concentrate device top
The steam of discharge is condensed through condenser, obtains 50% sulfuric acid.
By this equipment, the Efficient Cycle for realizing hydrogen chloride in PVC production processes is reclaimed.
The preferred embodiments of the present invention are the foregoing is only, the present invention is not limited to, for the skill of this area
For art personnel, the present invention can have various modifications and variations.It is all within the spirit and principles in the present invention, made any repair
Change, equivalent, improvement etc., should be included within the scope of the present invention.
Claims (6)
1. chlorination hydrogen recovery unit in a kind of PVC production processes, it is characterised in that described device includes：Hydrogen chloride combination is inhaled
Tower is received, described hydrogen chloride combined absorbing tower from bottom to top includes successively air inlet, discharging opening, isothermal uptake zone, and concentrated acid absorbs
Area, diluted acid uptake zone, clear water uptake zone and tower top exhaust outlet；The discharging opening is connected with concentrated acid tank, and the concentrated acid tank connects salt
Sour desorption device；The hydrochloric acid desorption device includes being provided with the discharge duct and diluted acid discharge line of drying device；The diluted acid
Discharge line connects watery hydrochloric acid desorption device.
2. chlorination hydrogen recovery unit in PVC production processes according to claim 1, it is characterised in that described isothermal is inhaled
Receive area and be provided with graphite falling film absorber.
3. chlorination hydrogen recovery unit in PVC production processes according to claim 1, it is characterised in that described concentrated acid is inhaled
Receipts area is packing area.
4. chlorination hydrogen recovery unit in PVC production processes according to claim 1, it is characterised in that described hydrochloric acid takes off
Inhaling device also includes hydrochloric acid head tank and sulfuric acid high position tank, the sulfuric acid high position tank connection extractant middle part.
5. chlorination hydrogen recovery unit in PVC production processes according to claim 4, it is characterised in that described extractor
Material be high temperature resistant and corrosion-resistant material, preferred high silicon ceramic material.
6. chlorination hydrogen recovery unit in PVC production processes according to claim 4, it is characterised in that on the extractor
Portion's tower body diameter is 1: 1.8-1: 2.5 with lower groove body diameter ratio.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710010325.1A CN106621715A (en) | 2017-01-06 | 2017-01-06 | Device for recovering chlorine hydride in PVC production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710010325.1A CN106621715A (en) | 2017-01-06 | 2017-01-06 | Device for recovering chlorine hydride in PVC production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106621715A true CN106621715A (en) | 2017-05-10 |
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ID=58844360
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710010325.1A Pending CN106621715A (en) | 2017-01-06 | 2017-01-06 | Device for recovering chlorine hydride in PVC production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106621715A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114917609A (en) * | 2022-06-17 | 2022-08-19 | 唐山三友氯碱有限责任公司 | Stripping system for removing low-content chloroethylene in PPVC (poly (vinyl chloride) latex |
-
2017
- 2017-01-06 CN CN201710010325.1A patent/CN106621715A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114917609A (en) * | 2022-06-17 | 2022-08-19 | 唐山三友氯碱有限责任公司 | Stripping system for removing low-content chloroethylene in PPVC (poly (vinyl chloride) latex |
| CN114917609B (en) * | 2022-06-17 | 2024-03-08 | 唐山三友氯碱有限责任公司 | Stripping system for removing low-content vinyl chloride in PPVC latex |
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| PB01 | Publication | ||
| PB01 | Publication | ||
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| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170510 |