CN211170533U - Continuous production device for water treatment agent HEDP - Google Patents
Continuous production device for water treatment agent HEDP Download PDFInfo
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- CN211170533U CN211170533U CN201921891829.XU CN201921891829U CN211170533U CN 211170533 U CN211170533 U CN 211170533U CN 201921891829 U CN201921891829 U CN 201921891829U CN 211170533 U CN211170533 U CN 211170533U
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Abstract
The utility model discloses a serialization apparatus for producing of water treatment agent HEDP specifically includes: mixing kettle, tubular reactor, vapour and liquid separator, hydrolysis kettle, outer cauldron of evaporating, acetic acid absorption tank and rectifying column, this device adopts phosphorus trichloride and acetic acid as the raw materials, through esterification, hydrolysis, outer continuous chemical process processing such as evaporating, realizes the whole recycle of raw materials acetic acid and byproduct acetic acid, effectively reduction in production cost. Meanwhile, hydrochloric acid and acetyl chloride are co-produced, so that the economic value is improved. Through continuous production, the equipment utilization rate is improved, the HEDP production yield is improved, the whole production process is performed in a closed manner, no waste is generated, and the method is green and environment-friendly.
Description
Technical Field
The utility model relates to a chemical industry equipment technical field especially relates to a serialization apparatus for producing of water treatment agent HEDP.
Background
Hydroxyethylidene diphenic acid (HEDP) is widely applied to an industrial circulating cooling water system as a water treatment agent. HEDP has good scale inhibition and corrosion inhibition effects, belongs to an anionic corrosion inhibitor, has better oxidation resistance than aminotrimethylene phosphate (ATMP), ethylene diamine tetramethylene sodium phosphate (EDTMP) and the like, and can be decomposed when the temperature reaches more than 250 ℃. HEDP also has good effect on inhibiting calcium carbonate, hydrated iron oxide and calcium phosphate, and can be used in combination with other corrosion inhibitors and scale inhibitors to achieve synergistic effect. Currently, the industrial production process of hydroxyethylidene diphenolic acid mainly comprises the following two processes: a synthesis process taking phosphorus trichloride, water and acetic acid as raw materials; a synthesis process taking phosphorous acid and acetic anhydride as raw materials. The two process routes have advantages and disadvantages respectively, the yield and the product quality of the second process are higher, but the raw material price is high, the process route is long, the operation requirement is strict, and the industrial production is limited. The first process adopts phosphorus trichloride, water and an acetic acid method to produce HEDP, which is an absolutely predominant production method in China and is also used by some foreign major companies.
The research on HEDP synthesis at home and abroad has already gained stage achievements, and the research mainly centers on the improvement of the batch process production technology of HEDP, the utility model adopts phosphorus trichloride and acetic acid as raw materials, provides a continuous production device of HEDP, and is favorable for the industrialized development of HEDP.
Disclosure of Invention
The utility model provides a serialization apparatus for producing of water treatment agent HEDP, this device coproduction acetyl chloride and hydrochloric acid, production system mesocycle is used can be got back to again to surplus acetic acid.
The continuous production device of the water treatment agent HEDP comprises a mixing kettle, a tubular reactor, a gas-liquid separator, a hydrolysis kettle, an outer steaming kettle and an acetic acid absorption tank which are sequentially connected in series, and is characterized in that an acetic acid feed port and PCl are arranged at the upper end of the mixing kettle3The feed inlet, the lower extreme is equipped with the mixing kettle discharge gate, the acetic acid feed inlet is connected with the acetic acid absorption tank and is formed closed loop pipeline, PCl3Feed inlet and PCl3The storage tanks are connected through pipelines, and a first shell-and-tube type constant temperature heat exchanger is arranged on the outer wall of the mixing kettle;
the tubular reactor comprises a tubular reactor feed inlet and a tubular reactor discharge outlet, the tubular reactor feed inlet is connected with the mixing kettle discharge outlet, the tubular reactor discharge outlet is connected with a gas-liquid separator, and the outer wall of the tubular reactor is provided with a second shell-and-tube type constant temperature heat exchanger;
the side wall of the gas-liquid separator is provided with a gas-liquid separator inlet, the upper end of the gas-liquid separator inlet is provided with a gas-liquid separator gas outlet, the lower end of the gas-liquid separator inlet is provided with a gas-liquid separator liquid outlet, the gas-liquid separator inlet is connected with the tubular reactor, the gas-liquid separator gas outlet is connected with the rectifying tower through a pipeline, and the gas-liquid separator liquid outlet is connected with the hydrolysis;
the upper end of the hydrolysis kettle is provided with a hydrolysis kettle feed inlet and a hydrolysis kettle water inlet, the lower end of the hydrolysis kettle is provided with a hydrolysis kettle discharge outlet, the hydrolysis kettle feed inlet is connected with a liquid outlet of the gas-liquid separator through a pipeline, the hydrolysis kettle water inlet is connected with a pure water pipeline through a pipeline, the hydrolysis kettle discharge outlet is connected with the outer steaming kettle through a pipeline, and the outer wall of the hydrolysis kettle is provided with a third shell-and-tube type constant temperature heat exchanger;
the upper end of the outer steaming kettle is provided with an outer steaming kettle feed inlet, an outer steaming kettle gas outlet and an outer steaming kettle water inlet, the lower end of the outer steaming kettle is provided with an outer steaming kettle discharge outlet, the outer steaming kettle feed inlet is connected with a hydrolysis kettle discharge outlet, the outer steaming kettle gas outlet is connected with an acetic acid absorption tank through a pipeline, the outer steaming kettle water inlet is connected with a pure water pipeline through a pipeline, the outer steaming kettle discharge outlet is connected with an HEDP dilution tank through a pipeline, the outer wall of the outer steaming kettle is provided with a fourth shell-and-tube type constant temperature heat exchanger,
acetic acid absorption tank upper end is equipped with acetic acid absorption tank air inlet and acetic acid absorption tank inlet, and the lower extreme is equipped with the acetic acid absorption tank discharge gate, the cauldron gas outlet is evaporated outward in the connection of acetic acid absorption tank air inlet, connect the acetic acid absorption tank discharge gate and connect the acetic acid feed inlet, the acetic acid absorption tank inlet passes through the pipe connection with the acetyl chloride storage tank.
Furthermore, first shell and tube type constant temperature heat exchanger is equipped with water inlet and delivery port, the water inlet passes through the pipeline with the cooling water inlet pipe and is connected in series with valve and circulating pump, the delivery port passes through the pipeline with the cooling water return pipe and is connected in series with the valve.
Furthermore, the second shell-and-tube type constant temperature heat exchanger, the third shell-and-tube type constant temperature heat exchanger and the fourth shell-and-tube type constant temperature heat exchanger are all provided with a steam inlet and a steam outlet, the steam inlets are all connected with the steam supply pipeline through pipelines and are connected with valves in series, and the steam outlets are all connected with the steam return pipeline through pipelines and are connected with valves in series.
Furthermore, the tubular reactor is made of graphite, the diameter of the tubular reactor is 50-100 cm, and the total length of the tubular reactor is 30-100 m, preferably 30-50 m.
Further, the acetic acid feed inlet of the mixing kettle and the PCl3The pipeline that feed inlet and corresponding head tank are connected is all established ties and is had valve, diaphragm pump and electron flowmeter on, it has valve, diaphragm pump and electron flowmeter to establish ties on the pipeline that mixing kettle discharge gate and tubular reactor feed inlet are connected.
Furthermore, a valve, a diaphragm pump and an electronic flowmeter are connected in series on a pipeline connecting the hydrolysis kettle feed inlet and the hydrolysis kettle water inlet with the corresponding device, and a valve and a transmission pump are connected in series on a pipeline connecting the hydrolysis kettle discharge outlet and the outer steaming kettle feed inlet.
Furthermore, a valve, a diaphragm pump and an electronic flowmeter are connected in series on a pipeline for connecting the water inlet of the outer steaming kettle with the pure water pipeline.
Furthermore, a valve, a diaphragm pump and an electronic flowmeter are connected in series on a pipeline connecting the liquid inlet of the acetic acid absorption tank and the acetyl chloride storage tank, and a valve and a negative pressure pump are connected in series on a pipeline connecting the air inlet of the acetic acid absorption tank and the air outlet of the outer steaming kettle.
Furthermore, the hydrolysis kettle and the external steaming kettle can be arranged in one group or a plurality of groups connected in parallel.
Further, the upper end of the rectifying tower is provided with an air outlet and is connected with the hydrochloric acid absorption tower through a pipeline, the side wall of the rectifying tower is provided with an air inlet connected with the air outlet of the gas-liquid separator, and the lower end of the rectifying tower is provided with a liquid outlet.
The invention has the advantages that
The utility model discloses the device has realized the whole recycle of raw materials acetic acid and byproduct acetic acid, effective reduction in production cost. Meanwhile, hydrochloric acid and acetyl chloride are co-produced, so that the economic value is improved. Through continuous production, the equipment utilization rate is improved, the HEDP production yield is improved, the whole production process is performed in a closed manner, no waste is generated, and the method is green and environment-friendly.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: 1. mixing kettle, 101, acetic acid feed inlet, 102, PCl3Feed inlet, 103, discharge outlet of mixing kettle, 2, tubular reactor, 201, feed inlet of tubular reactor, 202, discharge outlet of tubular reactor, 3, gas-liquid separator, 301, inlet of gas-liquid separator, 302, gas-liquid separator gas outlet, 303, gas-liquid separator liquid outlet, 4, hydrolysis kettle, 401, feed inlet of hydrolysis kettle, 402, water inlet of hydrolysis kettle, 403, discharge outlet of hydrolysis kettle, 5, external steaming kettle, 501, feed inlet of external steaming kettle, 502, gas outlet of external steaming kettle, 503, water inlet of external steaming kettle, 504, discharge outlet of external steaming kettle, 6, acetic acid absorption tank, 601, air inlet of acetic acid absorption tank, 602, liquid inlet of acetic acid absorption tank, 603, discharge outlet of acetic acid absorption tank, 7, fine acetic acid absorption tank, liquid inlet of acetic acid absorption tankThe system comprises a distillation tower, 701, an inlet, 702, an air outlet, 703, an air outlet, 8, a first shell-and-tube type constant temperature heat exchanger, 801, a first water inlet, 802, a first water outlet, 9, a second shell-and-tube type constant temperature heat exchanger, 901, a second air inlet, 902, a second air outlet, 10, a third shell-and-tube type constant temperature heat exchanger, 1001, a third air inlet, 1002, a third air outlet, 11, a fourth shell-and-tube type constant temperature heat exchanger, 1101, a fourth air inlet, 1102 and a fourth air outlet.
Detailed Description
The present application is further described with reference to the following description and detailed description of the preferred embodiments.
The continuous production device of the water treatment agent HEDP comprises a mixing kettle 1, a tubular reactor 2, a gas-liquid separator 3, a hydrolysis kettle 4, an outer steaming kettle 5 and an acetic acid absorption tank 6 which are sequentially connected in series, and is characterized in that an acetic acid feed port 101 and a PCl are arranged at the upper end of the mixing kettle3 A feed inlet 102, a mixing kettle discharge port 103 arranged at the lower end, an acetic acid feed inlet 101 connected with an acetic acid absorption tank to form a closed loop pipeline, and a PCl3Feed inlet 102 and PCl3The storage tanks are connected through pipelines, and the outer wall of the mixing kettle is provided with a first shell-and-tube type constant temperature heat exchanger 8;
the tubular reactor 2 comprises a tubular reactor feed inlet 201 and a tubular reactor discharge outlet 202, the tubular reactor feed inlet 201 is connected with the mixing kettle discharge outlet 103, the tubular reactor discharge outlet 202 is connected with the gas-liquid separator 3, and the outer wall of the tubular reactor is provided with a second shell-and-tube type constant temperature heat exchanger 9;
the side wall of the gas-liquid separator is provided with a gas-liquid separator inlet 301, the upper end of the gas-liquid separator is provided with a gas-liquid separator gas outlet 302, the lower end of the gas-liquid separator is provided with a gas-liquid separator liquid outlet 303, the gas-liquid separator inlet 301 is connected with the tubular reactor, the gas-liquid separator gas outlet 302 is connected with the rectifying tower 7 through a pipeline, and the gas-liquid separator liquid outlet 303 is connected with the hydrolysis kettle;
the upper end of the hydrolysis kettle is provided with a hydrolysis kettle feed inlet 401 and a hydrolysis kettle water inlet 402, the lower end of the hydrolysis kettle is provided with a hydrolysis kettle discharge outlet 403, the hydrolysis kettle feed inlet 401 is connected with a gas-liquid separator liquid outlet 303 through a pipeline, the hydrolysis kettle water inlet 402 is connected with a pure water pipeline through a pipeline, the hydrolysis kettle discharge outlet 403 is connected with an external steaming kettle through a pipeline, and the outer wall of the hydrolysis kettle is provided with a third shell-and-tube type constant temperature heat exchanger 10;
the upper end of the outer steaming kettle is provided with an outer steaming kettle feed inlet 501, an outer steaming kettle gas outlet 502 and an outer steaming kettle water inlet 503, the lower end of the outer steaming kettle is provided with an outer steaming kettle discharge outlet 504, the outer steaming kettle feed inlet 501 is connected with a hydrolysis kettle discharge outlet 403, the outer steaming kettle gas outlet 502 is connected with an acetic acid absorption tank through a pipeline, the outer steaming kettle water inlet 503 is connected with a pure water pipeline through a pipeline, the outer steaming kettle discharge outlet 504 is connected with an HEDP dilution tank through a pipeline, the outer wall of the outer steaming kettle is provided with a fourth shell-and-tube type constant temperature heat exchanger 11,
acetic acid absorption tank upper end is equipped with acetic acid absorption tank air inlet 601 and acetic acid absorption tank inlet 602, and the lower extreme is equipped with acetic acid absorption tank discharge gate 603, acetic acid absorption tank air inlet 601 connects outer cauldron gas outlet 502 that evaporates, connect acetic acid absorption tank discharge gate 603 and connect acetic acid feed inlet 101, acetic acid absorption tank inlet 602 passes through the pipe connection with the acetyl chloride storage tank.
Further, the first shell-and-tube type constant temperature heat exchanger 8 is provided with a water inlet and a water outlet, the water inlet 801 is connected with a cooling water inlet pipeline through a pipeline and is connected with a valve and a circulating pump in series, and the water outlet 802 is connected with a cooling water return pipeline through a pipeline and is connected with a valve in series.
Further, the second shell-and-tube type constant temperature heat exchanger 9, the third shell-and-tube type constant temperature heat exchanger 10 and the fourth shell-and-tube type constant temperature heat exchanger 11 are respectively provided with a steam inlet and a steam outlet, the steam inlets are respectively connected with the steam supply pipeline through pipelines and are connected in series with valves, and the steam outlets are respectively connected with the steam return pipeline through pipelines and are connected in series with valves.
Further, the tubular reactor 2 is made of graphite, the diameter is 50-100 cm, and the total length of the tubular reactor is 30-100 m, preferably 30-50 m.
Further, the mixing still acetic acid feed inlet 101 and the PCl3The pipeline of the feed inlet 102 connected with the corresponding raw material tank is connected with a valve, a diaphragm pump and an electronic flowmeter in series, and the discharge outlet 103 of the mixing kettle is connected with the pipeline of the corresponding raw material tankThe pipeline connected with the feed inlet 201 of the tubular reactor is connected in series with a valve, a diaphragm pump and an electronic flowmeter.
Furthermore, a valve, a diaphragm pump and an electronic flowmeter are connected in series on a pipeline connecting the hydrolysis kettle feed inlet 401 and the hydrolysis kettle water inlet 402 with the corresponding devices, and a valve and a transmission pump are connected in series on a pipeline connecting the hydrolysis kettle discharge outlet 403 with the outer steaming kettle feed inlet 501.
Furthermore, a valve, a diaphragm pump and an electronic flowmeter are connected in series on a pipeline connecting the water inlet 503 of the external steaming kettle and the pure water pipeline.
Further, a valve, a diaphragm pump and an electronic flowmeter are connected in series on a pipeline connecting the acetic acid absorption tank liquid inlet 602 and the acetyl chloride storage tank, and a valve and a negative pressure pump are connected in series on a pipeline connecting the acetic acid absorption tank gas inlet 601 and the outer steaming kettle gas outlet 502.
Further, the hydrolysis kettle 4 and the external steaming kettle 5 can be arranged in one group or multiple groups in parallel.
Further, the upper end of the rectifying tower is provided with an air outlet 702 and is connected with the hydrochloric acid absorption tower through a pipeline, the side wall of the rectifying tower is provided with an air inlet connected with the air outlet 302 of the gas-liquid separator, and the lower end of the rectifying tower is provided with a liquid outlet 703.
When the equipment is used, the HEDP production is carried out according to the following steps:
step 1, uniformly pumping into a mixing kettle 1 according to the flow quantity of 300L/h of acetic acid and 150L/h of phosphorus trichloride, simultaneously starting stirring, and controlling the temperature in the kettle to be less than 40 ℃ through a first shell-and-tube type constant temperature heat exchanger 8 on the outer wall of the mixing kettle.
And step 3: after a certain time, the reaction materials enter a gas-liquid separator 3 through a gas-liquid separator inlet 301 for separation, the mixed gas of acetyl chloride and hydrogen chloride enters a rectifying tower 7 from an upper end gas-liquid separator gas outlet 302 for further separation, and the intermediate product acetic ester enters a hydrolysis kettle through a lower end gas-liquid separator liquid outlet 303;
acetyl chloride in the rectifying tower enters an acetyl chloride storage tank from a liquid outlet 703 at the lower end of the rectifying tower, hydrogen chloride gas enters a hydrochloric acid absorption tower from an air outlet 702 at the upper end and is collected, and the temperature at the upper end of the rectifying tower is controlled below 35 ℃.
And 4, step 4: after the acetic ester enters the hydrolysis kettle, adding pure water into a water inlet 402 of the hydrolysis kettle according to a certain proportion for hydrolysis reaction, and controlling the temperature of a third shell-and-tube type constant temperature heat exchanger 10 in the reaction process to be 100-140 ℃ for 8-10 hours to obtain a mixed solution of HEDP and acetic acid.
And 5: the mixed liquid is transferred into an external steaming kettle 5 from a discharge port 403 of the hydrolysis kettle, negative pressure external steaming is carried out, acetic acid and a small amount of water enter an acetic acid absorption tank 6 from an air outlet 502 of the external steaming kettle in a gas state, and the rest HEDP is transferred into an HEDP storage tank from a discharge port 504 of the external steaming kettle after being diluted uniformly by adding quantitative pure water from an water inlet 503 of the external steaming kettle.
Step 6: quantitative acetyl chloride is added into an acetic acid liquid inlet 602 of the acetic acid absorption tank for water removal treatment, and then the acetic acid is used as an acetic acid raw material for recycling.
In one reaction cycle:
4698Kg of 60.5 percent HEDP aqueous solution is obtained, wherein the acetic acid content is 0.2 percent, the chloride ion content is 36ppm, the phosphorous acid content is 0.63 percent, and the phosphoric acid content is 12 ppm.
3896Kg of acetyl chloride as a by-product with purity of 99.12% is obtained.
3679Kg of hydrochloric acid as a by-product with a content of 32.85% is obtained.
The above-mentioned embodiments only express the embodiments of the present invention, and the description thereof is more specific and detailed, but not construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (10)
1. A continuous production device of a water treatment agent HEDP, which comprises a mixing kettle, a first reactor, a second reactor and a third reactor which are connected in series in sequence,The device comprises a tubular reactor, a gas-liquid separator, a hydrolysis kettle, an external steaming kettle and an acetic acid absorption tank and is characterized in that the upper end of the mixing kettle is provided with an acetic acid feed port and PCl3The feed inlet, the lower extreme is equipped with the mixing kettle discharge gate, the acetic acid feed inlet is connected with the acetic acid absorption tank and is formed closed loop pipeline, PCl3Feed inlet and PCl3The storage tanks are connected through pipelines, and a first shell-and-tube type constant temperature heat exchanger is arranged on the outer wall of the mixing kettle;
the tubular reactor comprises a tubular reactor feed inlet and a tubular reactor discharge outlet, the tubular reactor feed inlet is connected with the mixing kettle discharge outlet, the tubular reactor discharge outlet is connected with a gas-liquid separator, and the outer wall of the tubular reactor is provided with a second shell-and-tube type constant temperature heat exchanger;
the side wall of the gas-liquid separator is provided with a gas-liquid separator inlet, the upper end of the gas-liquid separator inlet is provided with a gas-liquid separator gas outlet, the lower end of the gas-liquid separator inlet is provided with a gas-liquid separator liquid outlet, the gas-liquid separator inlet is connected with the tubular reactor, the gas-liquid separator gas outlet is connected with the rectifying tower through a pipeline, and the gas-liquid separator liquid outlet is connected with the hydrolysis;
the upper end of the hydrolysis kettle is provided with a hydrolysis kettle feed inlet and a hydrolysis kettle water inlet, the lower end of the hydrolysis kettle is provided with a hydrolysis kettle discharge outlet, the hydrolysis kettle feed inlet is connected with a liquid outlet of the gas-liquid separator through a pipeline, the hydrolysis kettle water inlet is connected with a pure water pipeline through a pipeline, the hydrolysis kettle discharge outlet is connected with the outer steaming kettle through a pipeline, and the outer wall of the hydrolysis kettle is provided with a third shell-and-tube type constant temperature heat exchanger;
the upper end of the outer steaming kettle is provided with an outer steaming kettle feed inlet, an outer steaming kettle gas outlet and an outer steaming kettle water inlet, the lower end of the outer steaming kettle is provided with an outer steaming kettle discharge outlet, the outer steaming kettle feed inlet is connected with a hydrolysis kettle discharge outlet, the outer steaming kettle gas outlet is connected with an acetic acid absorption tank through a pipeline, the outer steaming kettle water inlet is connected with a pure water pipeline through a pipeline, the outer steaming kettle discharge outlet is connected with an HEDP dilution tank through a pipeline, and the outer wall of the outer steaming kettle is provided with a fourth shell-and-tube type constant temperature heat exchanger;
acetic acid absorption tank upper end is equipped with acetic acid absorption tank air inlet and acetic acid absorption tank inlet, and the lower extreme is equipped with the acetic acid absorption tank discharge gate, the cauldron gas outlet is evaporated outward in the connection of acetic acid absorption tank air inlet, the acetic acid feed inlet is connected to the acetic acid absorption tank discharge gate, the acetic acid absorption tank inlet passes through the pipe connection with the acetyl chloride storage tank.
2. The continuous production device of a water treatment agent HEDP in accordance with claim 1, wherein the first shell-and-tube type constant temperature heat exchanger has a water inlet and a water outlet, the water inlet is connected to a cooling water inlet pipe through a pipeline and is connected in series with a valve and a circulation pump, and the water outlet is connected to a cooling water return pipe through a pipeline and is connected in series with a valve.
3. The continuous production device of a water treatment agent HEDP according to claim 1, wherein the second, third and fourth shell-and-tube type constant temperature heat exchangers are provided with steam inlets and steam outlets, the steam inlets are connected with a steam supply pipeline through pipelines and are connected in series with valves, and the steam outlets are connected with a steam return pipeline through pipelines and are connected in series with valves.
4. The continuous production device of the water treatment agent HEDP of claim 1, wherein the tubular reactor is made of graphite, has a diameter of 50-100 cm, and has a total length of 30-100 m.
5. The continuous production device of the water treatment agent HEDP of claim 1, wherein the mixing kettle acetic acid feed inlet and PCl3The pipeline that feed inlet and corresponding head tank are connected is all established ties and is had valve, diaphragm pump and electron flowmeter on, it has valve, diaphragm pump and electron flowmeter to establish ties on the pipeline that mixing kettle discharge gate and tubular reactor feed inlet are connected.
6. The continuous production device of the water treatment agent HEDP of claim 1, wherein the pipelines connecting the feeding port of the hydrolysis kettle, the water inlet of the hydrolysis kettle and the corresponding devices are connected in series with a valve, a diaphragm pump and an electronic flow meter, and the pipelines connecting the discharging port of the hydrolysis kettle and the feeding port of the external steaming kettle are connected in series with a valve and a transmission pump.
7. The continuous production device of the water treatment agent HEDP of claim 1, wherein the pipeline connecting the water inlet of the external steaming kettle and the pure water pipeline is connected in series with a valve, a diaphragm pump and an electronic flow meter.
8. The continuous production device of the water treatment agent HEDP of claim 1, wherein a valve, a diaphragm pump and an electronic flowmeter are connected in series on a pipeline connecting the liquid inlet of the acetic acid absorption tank and the acetyl chloride storage tank, and a valve and a negative pressure pump are connected in series on a pipeline connecting the air inlet of the acetic acid absorption tank and the air outlet of the external steaming kettle.
9. The continuous production device of the water treatment agent HEDP of claim 1, wherein the hydrolysis kettle and the external steaming kettle can be arranged in one set or multiple sets in parallel.
10. The continuous production device of the water treatment agent HEDP in accordance with claim 1, wherein the rectifying tower has an outlet at the upper end and is connected to the hydrochloric acid absorption tower through a pipeline, the sidewall of the rectifying tower has an inlet connected to the outlet of the gas-liquid separator, and the lower end of the rectifying tower has an outlet.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201921891829.XU CN211170533U (en) | 2019-11-05 | 2019-11-05 | Continuous production device for water treatment agent HEDP |
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| CN201921891829.XU CN211170533U (en) | 2019-11-05 | 2019-11-05 | Continuous production device for water treatment agent HEDP |
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Address after: No.1, Shiliquan East Road, Shizhong District, Zaozhuang City, Shandong Province 277100 Patentee after: Shandong Taihe Technology Co.,Ltd. Address before: 277000 No.1, Shiliquan East Road, Shizhong District, Zaozhuang City, Shandong Province Patentee before: SHANDONG TAIHE WATER TREATMENT TECHNOLOGIES Co.,Ltd. |
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