CN215249583U

CN215249583U - Waste acid concentration regeneration sulfuric acid production line

Info

Publication number: CN215249583U
Application number: CN202121788298.9U
Authority: CN
Inventors: 叶世森; 彭德新; 高卫斌; 饶林杰
Original assignee: Jiujiang Fuda Industry Co ltd
Current assignee: Jiujiang Fuda Industry Co ltd
Priority date: 2021-08-03
Filing date: 2021-08-03
Publication date: 2021-12-21
Anticipated expiration: 2031-08-03

Abstract

The utility model relates to the technical field of waste acid treatment, in particular to a waste acid concentration and regeneration sulfuric acid production line, which comprises a pretreatment system, a double-effect evaporation system and a concentration system, wherein the pretreatment system comprises a raw material tank, a pretreatment tower, a dilution tank, a first filter, an active carbon adsorption tower, a carbon passing buffer tank, a second filter and a purification acid tank which are connected in sequence; the double-effect evaporation system comprises a preheating kettle, a double-effect evaporator, a double-effect intermediate tank, a single-effect evaporation kettle, a single-effect evaporator and a cooling buffer kettle which are connected in sequence, wherein the preheating kettle is connected with the purification acid tank; the concentration system comprises a concentration evaporator, a finished product cooling kettle and a finished product intermediate tank which are sequentially connected, wherein the concentration evaporator is connected with the cooling buffer kettle through a buffer pump. The utility model discloses can get rid of the waste material purification with the spent acid and carry out used repeatedly for concentrated sulfuric acid, the energy saving, reduction in production cost.

Description

Waste acid concentration regeneration sulfuric acid production line

Technical Field

The utility model relates to a spent acid treatment technical field especially relates to a concentrated regeneration sulphuric acid production line of spent acid.

Background

At present, 30 tons of waste acid is produced in the production process every day, the concentration of the waste acid is 52-53%, the waste acid contains a small amount of anthraquinone derivatives, bromine and water, the waste acid is dangerous waste, if the waste acid is discharged randomly, the ecological environment is damaged, the human health is influenced, and resources are wasted.

Based on the reason, the utility model provides a concentrated regeneration sulphuric acid production line of spent acid can get rid of the waste material purification with the spent acid and carry out used repeatedly for concentrated sulfuric acid, the energy saving, reduction in production cost.

SUMMERY OF THE UTILITY MODEL

The utility model aims to overcome prior art not enough, provide a concentrated regeneration sulphuric acid production line of spent acid, can get rid of the waste material purification with the spent acid and carry out used repeatedly for concentrated sulfuric acid, the energy saving, reduction in production cost.

In order to realize the utility model discloses a purpose, the utility model discloses a technical scheme do:

the utility model discloses a waste acid concentration regeneration sulfuric acid production line, which comprises a pretreatment system, a double-effect evaporation system and a concentration system,

the pretreatment system comprises a raw material tank, a pretreatment tower, a dilution tank, a first filter, an activated carbon adsorption tower, a carbon passing buffer tank, a second filter and a purification acid tank which are connected in sequence;

the double-effect evaporation system comprises a preheating kettle, a double-effect evaporator, a double-effect intermediate tank, a single-effect evaporation kettle, a single-effect evaporator and a cooling buffer kettle which are connected in sequence, wherein the preheating kettle is connected with the purification acid tank;

the concentration system comprises a concentration evaporator, a finished product cooling kettle and a finished product intermediate tank which are sequentially connected, wherein the concentration evaporator is connected with the cooling buffer kettle through a buffer pump.

The raw material tank is connected with the pretreatment tower through a raw material pump, and saturated steam generated by the pretreatment tower is introduced into tail gas treated by the pretreatment kettle and enters the first vacuum water tank; and the carbon passing buffer tank is input to the second filter through a carbon passing buffer pump.

The first effect evaporation kettle and the first effect evaporator are directly heated through saturated medium-pressure steam, steam hot water generated by the first effect evaporation kettle and the first effect evaporator is input to the preheating kettle for preheating, secondary steam generated by the preheating kettle is input to the second effect evaporator for heating, the secondary steam generated by the second effect evaporator enters the second vacuum water tank, and the second vacuum water tank is circularly cooled and neutralized through the cooler.

And the secondary steam generated by the concentration evaporator is washed by the purification tower and the condensation tower in sequence and then enters a vacuum system for cooling and neutralization.

The beneficial effects of the utility model reside in that:

(1) the utility model discloses can get rid of the waste material purification with the spent acid and carry out used repeatedly for concentrated sulfuric acid, the energy saving, reduction in production cost.

Drawings

Fig. 1 is a schematic structural diagram of the present invention.

In the figure: 1 head tank, 2 preliminary treatment towers, 3 dilution towers, 4 first filters, 5 activated carbon adsorption towers, 6 carbon buffer tanks, 7 second filters, 8 purification acid tanks, 9 preheating kettles, 10 double-effect evaporators, 11 double-effect intermediate tanks, 12 single-effect evaporation kettles, 13 single-effect evaporators, 14 cooling buffer kettles, 15 concentration evaporators, 16 finished product cooling kettles, 17 finished product intermediate tanks, 18 buffer pumps, 19 head pumps, 20 preliminary treatment kettles, 21 first vacuum water tanks, 22 carbon buffer pumps, 23 second vacuum water tanks, 24 coolers, 25 purification towers, 26 condensation towers, 27 vacuum systems.

Detailed Description

The following further description of the present invention:

referring to fig. 1 of the drawings, a drawing,

example (b):

a pretreatment system:

acid A (sulfuric acid concentration 52%, bromine concentration 0.5%) is conveyed from a raw material tank 1 to a pretreatment tower 2 through a raw material pump 19 by a flowmeter, saturated steam generated by the pretreatment tower 2 is introduced into a pretreatment kettle 20 to strip and blow bromine and simultaneously carry out a part of anthraquinone derivatives, and the temperature is controlled as follows: 128-132 ℃, and regulating a valve to control the vacuum degree: tail gas of-0.01 to-0.015 Mpa enters a first vacuum water tank 21 to be absorbed and neutralized, and condensed water contains partial anthraquinone derivatives and a small amount of sodium bromide generated by reaction with alkali liquor; the material acid overflow after pretreatment tower 2 handles gets into dilution tank 3 and dilutes to 25%, let the organic matter of part dissolution in sulphuric acid separate out, help improving adsorption effect, 3 intake of dilution tank are opened by flow control regulating valve, dilute for sour with the dilution pump get into active carbon adsorption tower 5 after 4 filters of first filter, put into deacidification jar washing deacidification and blow to the charcoal regeneration system with the charcoal after anthraquinone derivative absorption saturation, new charcoal after the regeneration is blown back new charcoal elevated tank cyclic utilization, it squeezes into the filtration of second filter 7 through 6 caches of charcoal buffer tank and gets into purification acid tank 8 and stores to cross charcoal acid.

Double-effect evaporation system:

directly heating saturated medium-pressure water vapor (2.0 Mpa, 220 ℃) to a first-effect evaporator 13 and a first-effect evaporation kettle 12, providing the preheating temperature of a preheating kettle 9 with the generated steam hot water to be 85-95 ℃, heating a second-effect evaporator 10 by the generated secondary steam, enabling the secondary steam generated by the second-effect evaporator 10 to enter a second vacuum water tank 23, circularly cooling and neutralizing the second vacuum water tank 23 by a cooler 24, wherein condensed water contains a part of anthraquinone derivatives and trace sodium bromide generated by reaction with alkali liquor;

the secondary evaporator 10 is negative pressure evaporation, and the vacuum degree is controlled: the purified acid A is preheated by a preheating kettle 9, then enters a secondary evaporator 10 for concentration (the temperature is 65-70 ℃, the vacuum degree is-0.088-minus 0.092 Mpa), overflows to a secondary intermediate tank 11, then is pumped into a primary evaporation kettle 12 (the temperature is 103-108 ℃, the pressure is-0.03-minus 0.035 Mpa), the acid in the primary evaporation kettle 12 overflows to a primary evaporator 13 for concentration to 80% (the temperature is 185-190 ℃, the pressure is-0.03-minus 0.035 Mpa), and then flows into a cooling buffer kettle 14 for cooling to 120-125 ℃.

A concentration system:

pumping the cooling buffer kettle 14 into a concentration evaporator 15 by using a buffer pump 18 for concentration to 92.5% (the temperature is 192-196 ℃, and the pressure is-0.094 to-0.096 Mpa), enabling concentrated sulfuric acid to pass through a finished product cooling kettle 16 and then enter a finished product intermediate tank 17 for storage, directly heating the concentration evaporator 15 by saturated medium-pressure water vapor (2.0 Mpa, 220 ℃), and preheating 9 the generated steam hot water by a preheating kettle;

the operation is carried out under negative pressure, secondary steam with 31 percent of azeotropic sulfuric acid content is generated and enters a purifying tower 25, after washing, the secondary steam enters a condensing tower 26 for deep cooling washing, then a vacuum system 27 is used for cooling and neutralization, and condensed water contains part of anthraquinone derivatives.

The above mentioned is only the embodiment of the present invention, not the limitation of the patent scope of the present invention, all the equivalent transformations made by the contents of the specification and the drawings or the direct or indirect application in the related technical field are included in the patent protection scope of the present invention.

Claims

1. A spent acid concentration regeneration sulphuric acid production line which is characterized in that: comprises a pretreatment system, a double-effect evaporation system and a concentration system,

the pretreatment system comprises a raw material tank (1), a pretreatment tower (2), a dilution tank (3), a first filter (4), an activated carbon adsorption tower (5), a carbon passing buffer tank (6), a second filter (7) and a purification acid tank (8) which are connected in sequence;

the double-effect evaporation system comprises a preheating kettle (9), a double-effect evaporator (10), a double-effect intermediate tank (11), a single-effect evaporation kettle (12), a single-effect evaporator (13) and a cooling buffer kettle (14) which are connected in sequence, wherein the preheating kettle (9) is connected with the purification acid tank (8);

the concentration system comprises a concentration evaporator (15), a finished product cooling kettle (16) and a finished product intermediate tank (17) which are connected in sequence, wherein the concentration evaporator (15) is connected with the cooling buffer kettle (14) through a buffer pump (18).

2. The spent acid concentration regeneration sulfuric acid production line of claim 1, wherein: the raw material tank (1) is connected with the pretreatment tower (2) through a raw material pump (19), saturated steam generated by the pretreatment tower (2) is introduced into tail gas treated by the pretreatment kettle (20) and enters a first vacuum water tank (21); the carbon passing buffer tank (6) is input to the second filter (7) through a carbon passing buffer pump (22).

3. The spent acid concentration regeneration sulfuric acid production line of claim 2, wherein: one effect evaporation cauldron (12) and one effect evaporimeter (13) are through saturated middling pressure steam direct heating, and the steam hot water input that both produced preheats cauldron (9) and preheats, the secondary steam input that preheats cauldron (9) produced extremely second effect evaporimeter (10) heating, the secondary steam that second effect evaporimeter (10) produced gets into second vacuum water tank (23), second vacuum water tank (23) are through cooler (24) circulative cooling and neutralization.

4. The spent acid concentration regeneration sulfuric acid production line of claim 3, wherein: the secondary steam generated by the concentration evaporator (15) enters a vacuum system (27) for cooling and neutralization after being washed by a purification tower (25) and a condensation tower (26) in sequence.