CN117018653B - Method for coproducing high-purity hydrogen chloride gas by high-temperature chloridizing chloropropene device - Google Patents
Method for coproducing high-purity hydrogen chloride gas by high-temperature chloridizing chloropropene device Download PDFInfo
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- CN117018653B CN117018653B CN202311015208.6A CN202311015208A CN117018653B CN 117018653 B CN117018653 B CN 117018653B CN 202311015208 A CN202311015208 A CN 202311015208A CN 117018653 B CN117018653 B CN 117018653B
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- 239000007789 gas Substances 0.000 title claims abstract description 120
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 53
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 title claims abstract description 42
- 229910000041 hydrogen chloride Inorganic materials 0.000 title claims abstract description 39
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000010992 reflux Methods 0.000 claims abstract description 47
- 239000007788 liquid Substances 0.000 claims abstract description 28
- 238000004821 distillation Methods 0.000 claims abstract description 23
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 18
- 239000002994 raw material Substances 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 238000001816 cooling Methods 0.000 claims description 21
- 238000000926 separation method Methods 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 5
- 238000011049 filling Methods 0.000 claims description 4
- 238000005660 chlorination reaction Methods 0.000 claims description 3
- 238000005057 refrigeration Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 22
- 238000001035 drying Methods 0.000 description 7
- 238000010025 steaming Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 150000008280 chlorinated hydrocarbons Chemical class 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 150000001805 chlorine compounds Chemical group 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 150000004678 hydrides Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005292 vacuum distillation 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
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/10—Preparation of halogenated hydrocarbons by replacement by halogens of hydrogen atoms
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0712—Purification ; Separation of hydrogen chloride by distillation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a method for co-producing high-purity hydrogen chloride gas by a high-temperature chloridizing method chloropropene device, and relates to the technical field of co-producing hydrogen chloride gas. The raw materials of the cold steam tower enter the cold steam tower after passing through a tertiary cold exchanger and a cold steam tower feeding precooler; the cold distillation tower top gas exchanges heat with the rectification tower top gas, then is divided into two parts after exchanging heat in a secondary cooler, and the top gas of the non-product part is dehydrated and washed after exchanging heat in a tertiary cooler; the top gas of the product is compressed by a rectification compressor, and then enters an HCL rectifying tower after being cooled by a second stage; the gas at the top of the rectifying tower is cooled into liquid by a primary cooler and then enters a reflux tank, and the pure propylene liquid at the bottom of the HCL rectifying tower can be directly recycled; the non-condensable gas is removed from the gas at the top of the rectifying tower in a reflux tank, and after being pressurized by a reflux pump, one part of the gas flows back to the HCL rectifying tower, and the other part of the gas is used for extracting hydrogen chloride. The method utilizes the surplus cold quantity of the original device to the maximum extent on the premise of not adding new refrigeration equipment, and increases the hydrogen chloride productivity.
Description
Technical Field
The invention relates to the technical field of co-production of hydrogen chloride gas, in particular to a method for co-producing high-purity hydrogen chloride gas by a high-temperature chloridizing method chloropropene device.
Background
The chloropropene process is that propylene with purity of more than 98% is dried, preheated to 280-320 ℃, and then sent into a mixer for mixing with cold chlorine according to a molar ratio of 4.5:1, and then sent into a reactor. The heat of reaction maintains the reaction temperature around 500 ℃. The propylene temperature is regulated by strictly controlling the raw material proportion so as to control the high-temperature chlorination reaction temperature and eliminate the phenomenon of carbon formation. The reaction product is chloride containing chloropropene, excessive chloropropene and hydride mixed gas, which is cooled to about 50 ℃ by a heat exchanger and a cooler, and then enters a prefractionator, the top of the prefractionator is refluxed by liquid, and the temperature is controlled to be-40 ℃, so that chlorinated hydrocarbons in the reaction gas are almost completely cooled and separated. The hydrogen chloride and unreacted propylene gas are sent out from the top of the tower to a propylene separation system. The hydrogen chloride in the gas can be washed and refined by water to obtain 35% hydrochloric acid material. Propylene is washed by water, neutralized and washed by alkali, enters a propylene compressor of 1.52-1.62MPa (gauge pressure), is cooled to become liquid, is cooled to 10 ℃ by a cooler, is dried to dew point-60 ℃ by a propylene drying tower (the water content is 10 mg/kg), is circulated and returned to a reaction system, and a crude chloropropene solution with 80 percent (weight) at the bottom of a prefractionator is subjected to light component removal by a refining tower, and the chloropropene product with the purity of 98 percent is obtained after heavy component removal, and the yield is 80-90 percent.
The hydrogen chloride and the excessive propylene gas generated by the high-temperature chlorination process are treated by adopting a secondary water washing and primary alkali washing mode, so that hydrochloric acid with the concentration of more than 30% is generated. The processing method has the following defects:
(1) The high-value (16000 yuan/ton-20000 yuan/ton) hydrogen chloride gas is not recovered, but only the low-value (400 yuan/ton) hydrochloric acid is generated;
(2) The propylene gas does not contain water originally, but in order to absorb the hydrogen chloride gas, the existing treatment method artificially adds water, so that the water content of the recovered propylene is high, and the energy of the subsequent treatment is increased;
(3) The separation of crude chloropropene and hydrogen chloride adopts a low-temperature distillation method, the temperature of the tower top is generally-40 ℃, and the cold energy of the tower top is not fully utilized by the existing treatment method, so that energy waste is caused.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a method for co-producing high-purity hydrogen chloride gas by a high-temperature chloridizing method chloropropene device.
Therefore, the technical scheme of the invention is that the method for coproducing high-purity hydrogen chloride gas by using the high-temperature chloridizing method chloropropene device comprises the following steps:
the raw materials of the cold steam tower sequentially pass through a tertiary cooler and a cold steam tower feeding precooler and then enter the cold steam tower;
the cold distillation tower top gas of the cold distillation tower exchanges heat with the rectifying tower top gas of the HCL rectifying tower, then is separated into product part top gas and non-product part top gas after exchanging heat in a secondary cooler, and the non-product part top gas is dehydrated and washed by the water after exchanging heat in a tertiary cooler;
the top gas of the product part after heat exchange in the secondary cooler is compressed by a rectification compressor, and the compressed top gas of the product part enters the HCL rectification tower after secondary cooling; the first-stage cooling is cooling by circulating water in a first-stage cooler of the compressor, and the second-stage cooling is cooling by cold steam overhead gas in a second-stage cooler;
the bottom of the HCL rectifying tower is heated by circulating water through a reboiler of the HCL rectifying tower, rectifying tower top gas of the HCL rectifying tower is cooled into liquid through a primary cooler and then enters a reflux tank, and the bottom of the HCL rectifying tower is pure propylene liquid and is directly recycled to the chloropropene device;
separating non-condensable gas from the rectifying tower top gas of the HCL rectifying tower in a reflux tank, pressurizing by a reflux pump, and refluxing one part of the non-condensable gas to the HCL rectifying tower and the other part of the non-condensable gas for extracting hydrogen chloride;
the non-condensable gas removed in the reflux tank is used for removing the water scrubber of the chloropropene device.
Preferably, the separation ratio of the top gas of the product part is 1% -5%.
Preferably, the temperature of the cold distillation tower top gas of the cold distillation tower after heat exchange with the rectification tower top gas of the HCL rectification tower is between minus 33 ℃ and minus 20 ℃, and the temperature of the cold distillation tower top gas after heat exchange in the secondary cooler is between minus 22 ℃ and minus 15 ℃.
Preferably, the cold distillation column top gas temperature of the cold distillation column is-40 ℃ to-25 ℃ and the pressure is 140kPa, and the content of HCL in the composition is 8% -15%.
Preferably, the number of plates of the HCL rectifying tower is 50-100, the tower pressure is 0.5-1.5MPa, the tower top temperature is-30 ℃ to-15 ℃, and the reflux ratio is 3-10.
A high-temperature chloridizing method chloropropene device comprises a tertiary cooler, a cold distillation tower feeding precooler, a cold distillation tower, a rectification compressor, a compressor primary cooler, a secondary cooler, an HCL rectification tower, a primary cooler, an HCL rectification tower reboiler, a reflux tank and a reflux pump.
Preferentially, the heat medium inlet of the third-time cold exchanger is connected with the raw material inlet of the cold steam tower, the heat medium outlet of the third-time cold exchanger is connected with the inlet of the feeding precooler of the cold steam tower, and the outlet of the feeding precooler of the cold steam tower is connected with the inlet of the cold steam tower.
Preferentially, an outlet of the cold steaming tower is connected with a cold medium inlet of the primary cold exchanger, a cold medium outlet of the primary cold exchanger is connected with a cold medium inlet of the secondary cold exchanger, a cold medium outlet of the secondary cold exchanger is respectively connected with an inlet of the rectifying compressor and a cold medium inlet of the tertiary cold exchanger, a cold medium outlet of the tertiary cold exchanger is connected with the water washing tower, an outlet of the rectifying compressor is connected with a heat medium inlet of the primary cooler of the compressor, a heat medium outlet of the primary cooler of the compressor is connected with a heat medium inlet of the secondary cold exchanger, and a heat medium outlet of the secondary cold exchanger is connected with a liquid inlet of the HCL rectifying tower.
Preferentially, the liquid outlet of the HCL rectifying tower is connected with the chloropropene device, the liquid outlet of the HCL rectifying tower is also connected with the liquid inlet of the HCL rectifying tower reboiler, the gas outlet of the HCL rectifying tower reboiler is connected with the gas inlet of the HCL rectifying tower, the gas outlet of the HCL rectifying tower is connected with the heat medium inlet of the primary cooler, and the heat medium outlet of the primary cooler is connected with the reflux tank.
Preferentially, the top outlet of the reflux tank is connected with the water scrubber, the bottom outlet of the reflux tank is connected with the reflux pump, and the outlet of the reflux pump is respectively connected with the HCL rectifying tower and the HCL filling equipment.
The invention has the beneficial effects that the cold energy utilization rate is improved, the investment is reduced, and the system running cost is reduced by adopting the cold energy tower top gas to carry out gradient utilization of the cold energy; the invention can fully utilize the cold energy of the cold steam overhead gas, and on the premise of not newly increasing refrigeration equipment, the invention maximally utilizes the surplus cold energy of the original device, thereby increasing the hydrogen chloride productivity; the bottom of the HCL rectifying tower is pure chloropropene liquid, does not contain water and has lower temperature, and can be directly recycled to a chloropropene device without drying, thereby reducing the cost of drying the chloropropene; the co-production of the high-purity hydrogen chloride product is increased, a part of hydrochloric acid product with low economic benefit is converted into high-quality hydrogen chloride product, and the economic benefit is considerable.
The invention adopts a mode of partially recycling the high-purity hydrogen chloride gas, and the high-purity hydrogen chloride gas with the annual output of 3 ten thousand tons of chloropropene can be coproduced by 600 tons of high-purity hydrogen chloride gas with the concentration of 99.9 percent, so that the cold energy is fully utilized, the investment is reduced, and the market competitiveness is higher.
Drawings
Fig. 1 is a schematic view of the overall structure of the present invention.
The symbols in the drawings illustrate:
1. a third cold exchanger; 2. feeding a precooler into a cold steaming tower; 3. a cold steaming tower; 4. rectifying the compressor; 5. a compressor primary cooler; 6. a secondary cooler; hcl rectifying column; 8. a primary cooler; a hcl rectifying column reboiler; 10. a reflux drum; 11. and a reflux pump.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
As shown in fig. 1, the invention provides a high-temperature chloridizing method chloropropene device, which comprises a tertiary cooler 1, a cold distillation tower feeding precooler 2, a cold distillation tower 3, a rectifying compressor 4, a compressor primary cooler 5, a secondary cooler 6, an HCL rectifying tower 7, a primary cooler 8, an HCL rectifying tower reboiler 9, a reflux tank 10 and a reflux pump 11.
The hot medium inlet of the third-time heat exchanger 1 is connected with the cold-steam tower raw material input port, the hot medium outlet of the third-time heat exchanger 1 is connected with the inlet of the cold-steam tower feeding precooler 2, the outlet of the cold-steam tower feeding precooler 2 is connected with the inlet of the cold-steam tower 3, the outlet of the cold-steam tower 3 is connected with the cold medium inlet of the primary heat exchanger 8, the cold medium outlet of the primary heat exchanger 8 is connected with the cold medium inlet of the secondary heat exchanger 6, the cold medium outlet of the secondary heat exchanger 6 is respectively connected with the inlet of the rectifying compressor 4 and the cold medium inlet of the third-time heat exchanger 1, the cold medium outlet of the third-time heat exchanger 1 is connected with the water washing tower, the outlet of the rectifying compressor 4 is connected with the hot medium inlet of the primary heat exchanger 5, the hot medium outlet of the primary heat exchanger 5 is connected with the liquid inlet of the secondary heat exchanger 6, the liquid outlet of the secondary heat exchanger 6 is connected with the chloropropene device, the liquid outlet of the secondary heat exchanger 6 is also connected with the liquid inlet of the cold-gas rectifying tower, the liquid outlet of the secondary heat exchanger is connected with the cold-gas reflux pump 10, the reflux pump 10 is connected with the cold-gas reflux inlet of the primary heat exchanger 8, and the reflux pump 10 is connected with the hot gas reflux inlet of the primary heat exchanger, and the reflux pump 10 is connected with the hot gas reflux pump 10.
The working principle of the invention is that the cold steam tower top gas of the cold steam tower 3 is divided into two parts after passing through the secondary cooler 6, one part is cooled in the tertiary cooler 1 and then is dehydrated and washed, the other part is a product part, the product part is cooled in a second stage after being pressurized by the rectification compressor 4, the first stage cooling is cooled in the first stage cooler 5 of the compressor through circulating water, the second stage cooling is cooled in the secondary cooler 6 through the cold steam tower top gas, then the cold steam tower top gas is rectified in the HCL rectifying tower 7, the tower top gas (HCL, N2) of the HCL rectifying tower is cooled in the primary cooler 8 and then condensed in the cold steam tower top gas to be removed in the reflux tank 10, the non-condensable gas (N2) is pressurized by the reflux pump 11, and then one part is refluxed to the HCL rectifying tower 7, and the other part is taken as liquid HCL product to remove HCL filling equipment. The non-condensable gas (N2) removed in the reflux drum 10 is removed from the water scrubber of the chloropropene device. The bottom of the HCL rectifying tower 7 is mainly propylene and high-boiling substances, and the propylene is directly recycled by a chloropropene removing device.
Based on the working principle, the invention provides a method for co-producing high-purity hydrogen chloride gas by a high-temperature chloridizing method chloropropene device,
1. the raw materials of the cold steaming tower sequentially pass through the three-time cold exchanger 1 and the cold steaming tower feeding precooler 2 and then enter the cold steaming tower 3, and the feeding temperature of the cold steaming tower 3 is-10 ℃.
2. The cold steam tower top gas of the cold steam tower 3 exchanges heat with the rectifying tower top gas of the HCL rectifying tower 7, then is separated into product part top gas and non-product part top gas after exchanging heat in the secondary cooler 6, the separation ratio of the product part top gas is 1% -5%, and the non-product part top gas is dehydrated and washed after exchanging heat in the tertiary cooler 1. The temperature of the cold steam tower top gas of the cold steam tower 3 is between minus 40 ℃ and minus 25 ℃ and the pressure is 140kPa, and the content of HCL in the composition is 8 to 15 percent; the temperature of the cold steam tower top gas of the cold steam tower 3 is between minus 33 ℃ and minus 20 ℃ after heat exchange with the rectifying tower top gas of the HCL rectifying tower 7, and the temperature is between minus 22 ℃ and minus 15 ℃ after heat exchange in the secondary cooler 6.
3. The top gas of the cold steam tower 3 is compressed by a rectification compressor 4 after heat exchange in a secondary cooler 6, and the compressed top gas of the product enters an HCL rectification tower 7 after secondary cooling. The first stage of cooling is cooling by circulating water in the first stage of cooler 5 of the compressor, and the second stage of cooling is cooling by cold steam overhead gas in the second cooler 6. The plate number of the HCL rectifying tower 7 is 50-100, the tower pressure is 0.5-1.5MPa, the tower top temperature is-30 ℃ to-15 ℃, and the reflux ratio is 3-10.
4. The bottom of the HCL rectifying tower 7 is heated by circulating water through a HCL rectifying tower reboiler 9, the rectifying tower top gas of the HCL rectifying tower 7 is cooled into liquid through a primary cooler 8 and then enters a reflux tank 10, the bottom of the HCL rectifying tower 7 is pure propylene liquid, and the liquid does not contain water and has low temperature, and can be directly recycled to a chloropropene device without drying.
5. The non-condensable gas (N2) is removed from the rectifying tower top gas of the HCL rectifying tower 7 in a reflux tank 10, and after the non-condensable gas is pressurized by a reflux pump 11, one part of the non-condensable gas is refluxed to the HCL rectifying tower 7, and the other part of the non-condensable gas is taken as a liquid HCL product to be taken as HCL filling equipment to extract hydrogen chloride.
6. The non-condensable gas (N2) removed in the reflux drum 10 is removed from the water scrubber of the chloropropene device.
The invention adopts the mode of self-cooling of the cold steam top gas to perform gradient utilization of cold energy, improves the utilization rate of the cold energy, reduces investment and reduces the running cost of the system.
In the prior art, the temperature of the cold distillation tower top gas of the chloropropene device is between minus 40 ℃ and minus 25 ℃ and is used for feeding and cooling the cold distillation tower, but the feeding temperature is minus 10 ℃, so that the cold quantity is high-quality and low-grade. The invention can fully utilize the partial cold energy, thereby saving the investment cost of the refrigerator and the operation cost. The bottom of the HCL rectifying tower 7 is pure propylene liquid, does not contain water and has lower temperature, and can be directly recycled to the chloropropene device without drying, thereby reducing the cost of drying the chloropropene. The co-production of the high-purity hydrogen chloride product is increased, a part of hydrochloric acid product with low economic benefit is converted into high-quality hydrogen chloride product, and the economic benefit is considerable.
The invention adopts a mode of partially recycling the high-purity hydrogen chloride gas, and the high-purity hydrogen chloride gas with the annual output of 3 ten thousand tons of chloropropene can be coproduced by 600 tons of high-purity hydrogen chloride gas with the concentration of 99.9 percent, so that the cold energy is fully utilized, the investment is reduced, and the market competitiveness is higher.
The economic benefit brought by the invention is calculated as follows:
(1) Benefit of the front face
1) Sales of hydrogen chloride gas (cylinder neglect):
600t/a 16000 yuan/t= 9600000 yuan/a
2) Propylene drying
The annual saving of the cold price is 51600 yuan/a calculated by 15kW and calculated by 0.43 yuan/kW
(2) Negative benefit
1) Reducing the yield of hydrochloric acid by 400 yuan/ton with the concentration of 30%
600/0.3=2000 tons/a
Hydrochloric acid selling price 2000 x 400=800000 yuan/a
2) Reducing the temperature of the top gas of the heavy component removal tower (utilizing the cold energy of the original device)
The annual cooling price is 464400 yuan/a based on 0.43 yuan/kW by using the cooling capacity of 135kW
(3) Total benefit
The total annual economic benefit is 8387200 yuan/a.
However, the foregoing description is only illustrative of the present invention and is not intended to limit the scope of the invention, so that the substitution of equivalent elements or equivalent variations and modifications within the scope of the invention are intended to fall within the scope of the claims.
Claims (7)
1. A method for co-producing high-purity hydrogen chloride gas by a high-temperature chloridizing method chloropropene device is characterized in that the high-temperature chloridizing method chloropropene device comprises a tertiary cooler, a cold distillation tower feeding precooler, a cold distillation tower, a rectification compressor, a compressor primary cooler, a secondary cooler, an HCL rectification tower, a primary cooler, an HCL rectification tower reboiler, a reflux tank and a reflux pump; the heat medium inlet of the tertiary cooler is connected with the raw material inlet of the cold steam tower, the heat medium outlet of the tertiary cooler is connected with the inlet of the feeding precooler of the cold steam tower, and the outlet of the feeding precooler of the cold steam tower is connected with the inlet of the cold steam tower; the outlet of the cold steam tower is connected with the cold medium inlet of the primary cooler, the cold medium outlet of the primary cooler is connected with the cold medium inlet of the secondary cooler, the cold medium outlet of the secondary cooler is respectively connected with the inlet of the rectifying compressor and the cold medium inlet of the tertiary cooler, the cold medium outlet of the tertiary cooler is connected with the water scrubber, the outlet of the rectifying compressor is connected with the heat medium inlet of the primary cooler of the compressor, the heat medium outlet of the primary cooler of the compressor is connected with the heat medium inlet of the secondary cooler, and the heat medium outlet of the secondary cooler is connected with the liquid inlet of the HCL rectifying tower;
the method comprises the following steps:
the raw materials of the cold steam tower sequentially pass through a tertiary cooler and a cold steam tower feeding precooler and then enter the cold steam tower;
the cold distillation tower top gas of the cold distillation tower exchanges heat with the rectifying tower top gas of the HCL rectifying tower, and then is separated into product part top gas and non-product part top gas after exchanging heat in a secondary cooler, and the non-product part top gas is dehydrated and washed by water after exchanging heat in a tertiary cooler;
the top gas of the product part of the cold steam tower subjected to heat exchange in the secondary cooler is compressed by a rectification compressor, and the compressed top gas of the product part is subjected to secondary cooling and then enters the HCL rectification tower; the first-stage cooling is cooling by circulating water in a first-stage cooler of the compressor, and the second-stage cooling is cooling by cold steam overhead gas in a second-stage cooler;
the bottom of the HCL rectifying tower is heated by circulating water through a reboiler of the HCL rectifying tower, rectifying tower top gas of the HCL rectifying tower is cooled into liquid through a primary cooler and then enters a reflux tank, and pure propylene liquid is formed at the bottom of the HCL rectifying tower and is directly recycled to a chloropropene device;
the non-condensable gas is removed from the rectifying tower top gas of the HCL rectifying tower in a reflux tank, and after the non-condensable gas is pressurized by a reflux pump, one part of the non-condensable gas is refluxed to the HCL rectifying tower, and the other part of the non-condensable gas is used for extracting hydrogen chloride;
and a water scrubber of the non-condensable gas chloropropene removal device removed in the reflux tank.
2. The method for co-producing high-purity hydrogen chloride gas by using a high-temperature chloridizing method chloropropene device according to claim 1, wherein the separation ratio of partial top gas of the product is 1% -5%.
3. The method for co-producing high purity hydrogen chloride gas by using high temperature chloridizing process chloropropene device according to claim 1, wherein the temperature of the cold distillation column top gas of the cold distillation column after heat exchange with the rectification column top gas of the HCL rectification column is-35 ℃ to-15 ℃, and the temperature of the cold distillation column top gas after heat exchange in the secondary cooler is-30 ℃ to-10 ℃.
4. The method for co-producing high purity hydrogen chloride gas by using high temperature chloridizing process chloropropene device according to claim 1, wherein the temperature of the cold distillation top gas of the cold distillation tower is-40 ℃ to-25 ℃, the pressure is 140kPa, and the content of HCL in the composition is 8% -15%.
5. The method for co-producing high purity hydrogen chloride gas by using high temperature chloridizing process chloropropene device according to claim 1, wherein the plate number of the HCL rectifying tower is 50-100, the tower pressure is 0.5-1.5MPa, the tower top temperature is-30 ℃ to-15 ℃, and the reflux ratio is 3-10.
6. The method for co-producing high-purity hydrogen chloride gas by using the high-temperature chlorination process chloropropene device according to claim 1, wherein the liquid outlet of the HCL rectifying tower is connected with the chloropropene device, the liquid outlet of the HCL rectifying tower is also connected with the liquid inlet of a reboiler of the HCL rectifying tower, the gas outlet of the reboiler of the HCL rectifying tower is connected with the gas inlet of the HCL rectifying tower, the gas outlet of the HCL rectifying tower is connected with the heat medium inlet of a primary cooler, and the heat medium outlet of the primary cooler is connected with a reflux tank.
7. The method for co-producing high-purity hydrogen chloride gas by using the high-temperature chloridizing method chloropropene device according to claim 6, wherein the top outlet of the reflux tank is connected with a water washing tower, the bottom outlet of the reflux tank is connected with a reflux pump, and the outlet of the reflux pump is respectively connected with an HCL rectifying tower and an HCL filling device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311015208.6A CN117018653B (en) | 2023-08-14 | 2023-08-14 | Method for coproducing high-purity hydrogen chloride gas by high-temperature chloridizing chloropropene device |
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| CN112521252A (en) * | 2020-12-13 | 2021-03-19 | 天津大学 | Concentrated heat pump rectification process and equipment for propargyl alcohol and butynediol aqueous solution system |
| WO2022155779A1 (en) * | 2021-01-19 | 2022-07-28 | 汇智工程科技股份有限公司 | Preparation process for epichlorohydrin |
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| CN103724158A (en) * | 2013-12-19 | 2014-04-16 | 山东海益化工科技有限公司 | Device for producing chloropropene |
| CN104926581A (en) * | 2014-03-21 | 2015-09-23 | 青岛科技大学 | Process flow for dry separation of propylene and hydrogen chloride |
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| WO2022155779A1 (en) * | 2021-01-19 | 2022-07-28 | 汇智工程科技股份有限公司 | Preparation process for epichlorohydrin |
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